US20110041551A1 - Process for separating off nitrogen - Google Patents

Process for separating off nitrogen Download PDF

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Publication number
US20110041551A1
US20110041551A1 US12/851,149 US85114910A US2011041551A1 US 20110041551 A1 US20110041551 A1 US 20110041551A1 US 85114910 A US85114910 A US 85114910A US 2011041551 A1 US2011041551 A1 US 2011041551A1
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Prior art keywords
fraction
double
process according
hydrocarbon
heat exchangers
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Abandoned
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US12/851,149
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English (en)
Inventor
Heinz Bauer
Rainer Sapper
Andreas Bub
Stephan Burmberger
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Linde GmbH
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Linde GmbH
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Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BUB, ANDREAS, SAPPER, RAINER, BAUER, HEINZ, BURMBERGER, STEPHAN
Publication of US20110041551A1 publication Critical patent/US20110041551A1/en
Abandoned legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • 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
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • 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
    • F25J3/0257—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/08—Processes or apparatus using separation by rectification in a triple pressure main column 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/38—Processes or apparatus using separation by rectification using pre-separation or distributed distillation before a main column system, e.g. in a at least a double column 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

Definitions

  • the invention relates to a process for separating off C 2+ -hydrocarbons from a feed fraction containing essentially nitrogen and hydrocarbons, wherein
  • a process of the type in question for separating off C 2+ -hydrocarbons from a feed fraction containing essentially nitrogen and hydrocarbons is known, for example, from U.S. Pat. No. 4,664,686.
  • FIG. 1 which essentially corresponds to FIG. 3 of the abovementioned U.S. patent, a description will be given hereinafter of the process of the type in question for separating off C 2+ -hydrocarbons from a feed fraction containing essentially nitrogen and hydrocarbons.
  • a feed fraction containing essentially nitrogen and hydrocarbons and which originates, for example, from an oil degassing or LNG plant which is not shown in the FIG. 1 is introduced into heat exchanger E 1 .
  • the feed fraction (petroleum associated gas or light expansion gas) preferably has a pressure of above 25 bar. It has optionally already been subjected to a pretreatment, such as desulphurization and/or drying.
  • the feed fraction is cooled and partially condensed against process streams which will be considered in more detail hereinafter.
  • the partially condensed feed fraction is taken off from the heat exchanger E 1 and, via the expansion valve a, introduced into a separation column T.
  • the abovementioned separation column T serves for this purpose.
  • a low-nitrogen, C 2+ -rich hydrocarbon fraction is separated off from the feed fraction, which C 2+ -rich hydrocarbon fraction is taken off from the bottom of the separation column T via the line 5 , cold-producingly expanded in the valve b and, after warming and vaporization in the heat exchanger E 1 , is released via line 5 ′ as what is termed a medium-pressure hydrocarbon fraction.
  • a substream of this liquid fraction is taken off from the bottom of the separation column T, and, after a cold-producing expansion in the valve c, is added via the line 6 to the methane-rich fraction taken off from the double-column process N, and thus serves for providing cold in the top condenser E 2 .
  • This methane-rich fraction will be considered in more detail hereinafter.
  • a C 2+ -hydrocarbon-depleted fraction is taken off, which fraction has a higher nitrogen content compared with the feed fraction introduced in the line 1 .
  • This C 2+ -hydrocarbon-depleted fraction is partially condensed in the heat exchanger or top condenser E 2 and fed to the separator D via the line 2 ′.
  • the liquid fraction occurring is taken off and fed as reflux to the column T.
  • a return pump P must be provided in the line 3 . This can be omitted if the separator D is arranged above the feed-in point of the reflux stream.
  • the C 2+ -hydrocarbon-depleted gas fraction removed from the separator D is fed via line 4 to a double-column process N which is shown only schematically.
  • double-column processes are sufficiently known to those skilled in the art from the prior art.
  • a prior art double-column process is described, for example, in the German patent application 10 2009 008229 which was not published before the priority date of the present application. By citing the German patent application 10 2009 008229, the contents thereof are hereby fully incorporated into the contents of the present patent application.
  • the bottom of the separation column T is heated by means of a bottom heater integrated into the heat exchanger E 1 —shown by the pipe sections 9 and 9 ′.
  • the nitrogen-rich fraction obtained in the double-column process N is removed via line 8 , warmed in the heat exchanger E 1 against the feed fraction to be cooled, and then fed via line 8 ′ to a further use thereof.
  • the methane-rich fraction obtained in the double-column process N is fed via line 7 to the top condenser E 2 —if appropriate after previous addition of a substream of the liquid fraction taken off in the separation column T—warmed therein and vaporized, at least in part, subsequently fed via line 7 ′ to the heat exchanger E 1 , and, after further warming and complete vaporization against the feed fraction to be cooled, is fed via line 7 ′′ to further use thereof.
  • the main feature is directed towards optimizing the flow rate of the C 2+ -hydrocarbon fraction removed from the bottom of the separation column T in order to be able to release this at elevated pressure via the lines 5 and 5 ′.
  • the remaining hydrocarbons are released at a lower pressure via the line 7 ′′ in this procedure. Since both hydrocarbon fractions 5 ′/ 7 ′′ are to be released together, it is necessary to compress at least one of the two fractions, customarily fraction 7 ′′, to the desired release pressure—this compression is not shown in FIG. 1 .
  • the composition of the liquid fraction 5 taken off from the bottom of the separation column T is optimized to a low nitrogen content.
  • the composition of the gas fraction taken off from the top of the separation column T in contrast, is optimized to a nitrogen content as high as possible, but not in respect of the hydrocarbon composition, in particular a high methane content.
  • the methane-rich stream taken off from the double-column process N in this case must be set such that it can fulfil its tasks in the heat integration at a pressure as high as possible.
  • an aspect of the present invention is to provide a process of the type mentioned above, for separating off C 2+ -hydrocarbons from a feed fraction containing essentially nitrogen and hydrocarbons, which avoids the disadvantages described.
  • This aspect can be achieved according to the invention by a process for separating off C 2+ -hydrcarbons from a feed fraction containing essentially nitrogen and hydrocarbons, wherein the liquid fraction, obtained from the partial condensation of the C 2+ -hydrocarbon-depleted fraction removed from the top of the separation column T, is fed at least in part, together with the C 2+ -hydrocarbon-depleted gas fraction, to the double-column process, and is separated therein into a nitrogen-rich fraction and a methane-rich fraction.
  • FIG. 1 schematically illustrates an exemplary embodiment of the prior art
  • FIGS. 2 and 3 each illustrate exemplary embodiments of the process according to the invention.
  • the liquid separated in the separator D is fed according to the invention, in part, via line 10 and expansion valve d to the double-column process N.
  • the remaining part of the liquid from separator D is fed to the separation column T via line 3 as reflux stream.
  • the energy balance thereof is altered in such a manner that the methane-rich stream taken off from the double-column process N via line 7 is completely liquid, instead of partially vaporized as in previous systems.
  • sufficient cold capacity is available to the top condenser E 2 even without the addition, shown in FIG. 1 , of a substream of the liquid fraction taken off from the bottom of the separation column T.
  • the liquid fraction taken off from the bottom of the separation column T via line 11 is therefore, after expansion in the valve e, added to the methane-rich fraction between the top condenser E 2 and heat exchanger E 1 .
  • the liquid fraction taken off via line 11 is therefore advantageously only used for precooling the feed fraction in the heat exchanger E 1 .
  • the required temperature profile of the overall process can therefore be provided by hydrocarbons vaporizing essentially isobarically—this means that only conventional pressure drops occur of in total a maximum of 1 bar in the heat exchangers E 2 and E 1 .
  • the fraction taken off via line 2 from the top of the separation column T is now freed as far as possible C 2+ -hydrocarbons and carbon dioxide.
  • the methane-rich stream taken off from the double-column process N via line 7 thus has a significantly higher methane content than that in the procedure shown in FIG. 1 .
  • the operation of the separation column T is optimized to the effect that the content of C 2+ -hydrocarbons in the fraction taken off via line 2 from the top of the separation column T is a maximum of 0.1% by volume (1000 vppm), preferably a maximum of 0.01% by volume (100 vppm).
  • the process procedure shown in FIG. 3 differs from that shown in FIG. 2 essentially in that the multipipe heat exchanger E 1 is divided into a plurality of double-pipe heat exchangers E 1 , E 1 ′ and E 3 . In addition, an additional separator D′ is provided. Such a process procedure makes it possible to ensure stable flow conditions in the heat exchangers in a wide range of feed fraction composition and load states.
  • the feed fraction is divided into two substreams 1 and 20 . Both are cooled and partially condensed in the heat exchangers E 1 and E 1 ′, respectively.
  • the first substream 1 is fed in a known manner to the separation column T via line 1 ′ and expansion valve a.
  • the second substream 20 is fed to the heat exchanger E 3 via line 20 ′ and subsequently separated in the separator D′ into a liquid fraction and a gas fraction.
  • a hydrocarbon-rich fraction is removed from separation column T via line 30 at a suitable point, warmed in a heat exchanger E 3 and also partially vaporized and then fed via line 30 ′ to the separation column T.
  • the gaseous fraction taken off via line 22 from the separator D′ is cooled in the heat exchanger E 1 ′, partially condensed and subsequently fed via line 22 ′ and expansion valve f to the separation column T.
  • the operation of the separation column T can be varied or optimized.
  • the above-described heat exchangers E 1 and E 1 ′ are advantageously constructed as helically coiled heat exchangers, wherein the cooling or partial condensation of the feed fractions proceeds in the tubes and the vaporization or warming of the cold fractionation products proceeds on the shell side of the helically coiled heat exchangers.
  • the cooling or partial condensation of the feed fraction preferably proceeds in an ascending manner on the tube side and the warming or vaporization of the fractionation products proceeds in a falling manner on the shell side.
  • top condenser E 2 is constructed as a circulation evaporator, complete vaporization of the methane-rich fraction removed from the double-column process N via line 7 can be achieved in a controlled manner. From this circulation vessel having a controlled liquid level in which the top condenser E 2 is arranged, the fraction 7 ′ is thereby taken off exclusively in the gaseous state.
US12/851,149 2009-08-06 2010-08-05 Process for separating off nitrogen Abandoned US20110041551A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102009036366.1 2009-08-06
DE102009036366A DE102009036366A1 (de) 2009-08-06 2009-08-06 Verfahren zum Abtrennen von Stickstoff

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US20110041551A1 true US20110041551A1 (en) 2011-02-24

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US12/851,149 Abandoned US20110041551A1 (en) 2009-08-06 2010-08-05 Process for separating off nitrogen

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US (1) US20110041551A1 (es)
AU (1) AU2010202696B2 (es)
DE (1) DE102009036366A1 (es)
MX (1) MX337989B (es)
NO (1) NO20101115A1 (es)
RU (1) RU2537110C2 (es)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11604024B2 (en) 2017-12-21 2023-03-14 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method for producing pure nitrogen from a natural gas stream containing nitrogen

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015001858A1 (de) * 2015-02-12 2016-08-18 Linde Aktiengesellschaft Kombinierte Abtrennung von Schwer- und Leichtsiedern aus Erdgas

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4455158A (en) * 1983-03-21 1984-06-19 Air Products And Chemicals, Inc. Nitrogen rejection process incorporating a serpentine heat exchanger
US4519824A (en) * 1983-11-07 1985-05-28 The Randall Corporation Hydrocarbon gas separation
US4664686A (en) * 1986-02-07 1987-05-12 Union Carbide Corporation Process to separate nitrogen and methane
US4710212A (en) * 1986-09-24 1987-12-01 Union Carbide Corporation Process to produce high pressure methane gas
US5183101A (en) * 1991-05-21 1993-02-02 Bio-Rad Laboratories, Inc. Circulating chiller for electrified solutions
US5617741A (en) * 1995-02-10 1997-04-08 Air Products And Chemicals, Inc. Dual column process to remove nitrogen from natural gas

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009008229A1 (de) 2009-02-10 2010-08-12 Linde Ag Verfahren zum Abtrennen von Stickstoff

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4455158A (en) * 1983-03-21 1984-06-19 Air Products And Chemicals, Inc. Nitrogen rejection process incorporating a serpentine heat exchanger
US4519824A (en) * 1983-11-07 1985-05-28 The Randall Corporation Hydrocarbon gas separation
US4664686A (en) * 1986-02-07 1987-05-12 Union Carbide Corporation Process to separate nitrogen and methane
US4710212A (en) * 1986-09-24 1987-12-01 Union Carbide Corporation Process to produce high pressure methane gas
US5183101A (en) * 1991-05-21 1993-02-02 Bio-Rad Laboratories, Inc. Circulating chiller for electrified solutions
US5617741A (en) * 1995-02-10 1997-04-08 Air Products And Chemicals, Inc. Dual column process to remove nitrogen from natural gas

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11604024B2 (en) 2017-12-21 2023-03-14 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method for producing pure nitrogen from a natural gas stream containing nitrogen

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AU2010202696B2 (en) 2016-02-25
MX337989B (es) 2016-03-30
RU2010132951A (ru) 2012-02-10
MX2010007252A (es) 2011-02-07
NO20101115A1 (no) 2011-02-07
AU2010202696A1 (en) 2011-01-20
DE102009036366A1 (de) 2011-02-10
RU2537110C2 (ru) 2014-12-27

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