WO2002088612A1 - Verfahren zum abtrennen von stickstoff aus einer stickstoff-enthaltenden, kohlenwasserstoff-reichen fraktion - Google Patents
Verfahren zum abtrennen von stickstoff aus einer stickstoff-enthaltenden, kohlenwasserstoff-reichen fraktion Download PDFInfo
- Publication number
- WO2002088612A1 WO2002088612A1 PCT/EP2002/004721 EP0204721W WO02088612A1 WO 2002088612 A1 WO2002088612 A1 WO 2002088612A1 EP 0204721 W EP0204721 W EP 0204721W WO 02088612 A1 WO02088612 A1 WO 02088612A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- hydrocarbon
- nitrogen
- rich
- circuit
- fraction
- Prior art date
Links
Classifications
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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
- F25J3/0257—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
-
- 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
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
-
- 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
- F25J2210/04—Mixing or blending of fluids with 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/90—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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
-
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
-
- 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
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- 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
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/20—Integration in an installation for liquefying or solidifying a fluid 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
-
- 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
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2280/00—Control of the process or apparatus
- F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
Definitions
- the invention relates to the combination of a
- double-column nitrogen separation process should be understood to mean the most varied of nitrogen separation processes, i.e. regardless of whether it is a pure double-column process, a double-column process with separation of the heavy hydrocarbons, a double-column process with a nitrogen enrichment column with or without separation heavy hydrocarbons, a single column process with or without pre-separation of heavy hydrocarbons, etc.
- the compression of the refrigerant or refrigerant or refrigerant mixture circulating in the refrigerant circuits and / or refrigerant (mixture) circuits is carried out by means of energy-intensive compressors.
- gas turbines are provided which, as a rule, have previously been fed by a partial stream of the hydrocarbon-rich stream to be liquefied.
- the distribution systems and thus the fuel gas of such gas turbines can tolerate comparatively high nitrogen concentrations, they have the disadvantage that the NO x content of their exhaust gas is comparatively high, ie for example> 25 mol-ppm NO x .
- low-NO x gas turbines these are gas turbines which are equipped with a so-called “dry-low-NO ⁇ -emission-Co ⁇ bustion system", but which must be operated with a comparatively low-nitrogen gas mixture .
- the maximum nitrogen content of the fuel gas supplied to the turbines should not exceed 10 - 30 mol%, depending on the turbine type, in order to achieve the desired NO x limit value of max. Not to exceed 25 mole ppm for the gas turbine exhaust gas.
- the so-called specific gravity and the Wobbe index of the hydrocarbon-rich fuel gas are limited to, for example, ⁇ 1% within, for example, 30 seconds are, because only in this way stable operation of the gas turbine can be guaranteed without it being, for. B. instabilities with regard to the flame.
- the object of the present invention is to provide a generic method combination which enables a reduction in the energy consumption of the nitrogen separation process while at the same time reducing its investment costs.
- the hydrocarbon-rich stream is liquefied by indirect heat exchange with the refrigerants of a refrigerant mixture circuit cascade, the refrigerant mixture circuit cascade consisting of at least 3 different refrigerant mixture circuits with different refrigerant compositions, and the first of the three refrigerant mixture circuits of the pre-cooling (precooling circuit), the second refrigerant circuit and the third refrigerant mixture circuit is used for subcooling (subcooling circuit) of the hydrocarbon-rich stream to be liquefied, then - in accordance with an advantageous embodiment of the process combination according to the invention - the cooling and partial condensation of the nitrogen-containing, hydrocarbon-rich fraction takes place against the precooling circuit and the subcooling circuit Process for liquefying the hydrocarbon rich hen electricity.
- Figure 1 a three-stage compressor unit, which serves to compress the nitrogen-containing, hydrocarbon-rich stream
- Figure 2 a possible embodiment of a double column nitrogen separation process.
- a nitrogen-containing, hydrocarbon-rich fraction is fed via line 1 to a three-stage compressor unit - the three stages of the compressor unit are designated V1, V2 and V3. This can arise from any that arise within the respective liquefaction process
- Compound nitrogen-containing, hydrocarbon-rich streams for example from a nitrogen stripper, boil-off gas, etc.
- the nitrogen-containing, hydrocarbon-rich fraction can at least temporarily be mixed with a nitrogen-rich stream via line 2 - which will be discussed in more detail below.
- the nitrogen-containing, hydrocarbon-rich fraction, to which the nitrogen-rich stream brought in via line 2 was optionally added, is fed via line 3 to the first compressor stage V1 at a slightly above atmospheric pressure. After compression, this fraction is one via line 4
- the nitrogen-containing, hydrocarbon-rich fraction drawn off from the compressor unit via line 6 has a pressure between 35 and 65 bar at a temperature of 5 to 40 ° C.
- the nitrogen-containing, hydrocarbon-rich fraction drawn off from the compressor unit is now - as shown in FIG. 2 below - in the heat exchanger E4 against the high-purity nitrogen stream which is fed to the heat exchanger E4 via line 16 and is discussed in more detail below are cooled, and according to the invention against a refrigerant (mixture) stream x to a temperature between -20 and -60 ° C.
- the heat exchangers E4 to E7 shown in FIG. 2 are preferably designed as so-called plate heat exchangers.
- the nitrogen-containing, hydrocarbon-rich fraction is then fed via line 8 to a further heat exchanger E5 and in this again in turn against the already mentioned high-purity nitrogen stream in line 15 and another refrigerant (mixture) stream y to a temperature between -80 and cooled to -120 ° C.
- the process for liquefying a hydrocarbon-rich stream is a refrigerant mixture circuit cascade process
- the nitrogen-containing, hydrocarbon-rich fraction is then fed via line 9 to the heat exchanger E6, in which it is heated to a temperature of - against a reboiler which is drawn off from the lower column a of the double column K via line 11 and which is subsequently fed back in again. Cooled to 120 to -140 ° C. before the nitrogen-containing, hydrocarbon-rich fraction is fed via line 10 to the lower column a of the double column K.
- the lower column a has a working pressure of approximately 30 bar.
- a nitrogen-depleted, hydrocarbon-rich fraction is drawn off from the bottom of the lower column a and is cooled to a temperature between -155 and -160 ° C. in the heat exchanger E5 already described before this fraction is fed via line 13 and expansion valve 13 'the upper column b of the double column K is abandoned.
- the upper column b has a working pressure of approximately 2 bar.
- a nitrogen-enriched, hydrocarbon-rich liquid or, if appropriate, gas fraction is drawn off via line 14, cooled in the heat exchanger E7, where appropriate partially condensed and returned to the top of the upper column b given the double column K.
- the already mentioned high-purity nitrogen gas fraction which has a residual hydrocarbon content of z. B. ⁇ 100 ppm and a temperature of -190 ° C, deducted.
- This gas fraction is first heated in the heat exchanger E7 and then fed to the already described heat exchangers E4 and E5 and heated therein to the nitrogen-containing, hydrocarbon-rich fraction which is fed to the double column K for separation.
- the heated high-purity nitrogen gas fraction can be sent via line 17 to the
- a partial stream of this gas fraction can also be returned to the compressor station V1 to V3 via line 2.
- This procedure serves to keep the nitrogen content of the gas fraction fed to the compressor station V1 to V3 above a desired or required minimum concentration of, for example, 15%. If this minimum concentration were not reached, the desired nitrogen purity in the stream released into the atmosphere could not be achieved without an additional pre-separation step.
- the operation of the method according to the invention is simplified and stabilized, since the fluctuations in the gas fraction fed to the compressor station V1 to V3 can be minimized with regard to the nitrogen content. However, this is only possible at the expense of higher energy consumption.
- a methane-rich liquid fraction is drawn off from the lower region of the upper column b of the double column K and can be fed, for example, to a nitrogen stripping column - which is integrated, for example, in an LNG process. This can be done either by gravity or by pumping the liquid.
- the methane-rich liquid fraction preferably has a nitrogen content of at most 5% by volume.
- the refrigeration is now provided according to the invention by the two refrigerant circuits or refrigerant mixture cycles x and y.
- the cooling and partial condensation of the nitrogen-containing, hydrocarbon-rich stream to be separated can of course also take place against only one refrigerant stream or refrigerant mixture stream. This allows the hydrocarbon-rich electricity to be withdrawn from the process or the system in liquid form (see side draw via line 18).
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- 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)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2002319155A AU2002319155B2 (en) | 2001-05-02 | 2002-04-29 | Method for separating nitrogen out of a hydrocarbon-rich fraction that contains nitrogen |
NO20034865A NO20034865L (no) | 2001-05-02 | 2003-10-31 | Fremgangsmåte for å separere ut nitrogen fra en nitrogenholdig hydrokaronrik fraksjon |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10121339.5 | 2001-05-02 | ||
DE2001121339 DE10121339A1 (de) | 2001-05-02 | 2001-05-02 | Verfahren zum Abtrennen von Stickstoff aus einer Stickstoff-entaltenden Kohlenwasserstoff Fraktion |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2002088612A1 true WO2002088612A1 (de) | 2002-11-07 |
Family
ID=7683369
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2002/004721 WO2002088612A1 (de) | 2001-05-02 | 2002-04-29 | Verfahren zum abtrennen von stickstoff aus einer stickstoff-enthaltenden, kohlenwasserstoff-reichen fraktion |
Country Status (4)
Country | Link |
---|---|
AU (1) | AU2002319155B2 (de) |
DE (1) | DE10121339A1 (de) |
NO (1) | NO20034865L (de) |
WO (1) | WO2002088612A1 (de) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7520143B2 (en) | 2005-04-22 | 2009-04-21 | Air Products And Chemicals, Inc. | Dual stage nitrogen rejection from liquefied natural gas |
WO2010094396A3 (de) * | 2009-02-19 | 2013-04-18 | Linde Aktiengesellschaft | Verfahren zum abtrennen von stickstoff |
RU2537486C2 (ru) * | 2009-08-21 | 2015-01-10 | Линде Акциенгезелльшафт | Способ сжижения обогащенной углеводородами, содержащей азот сырьевой фракции, предпочтительно природного газа |
WO2014173598A3 (en) * | 2013-04-22 | 2015-12-03 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for producing a liquefied hydrocarbon stream |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102007007097A1 (de) * | 2007-02-13 | 2008-08-14 | Linde Ag | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
FR2991442B1 (fr) * | 2012-05-31 | 2018-12-07 | L'air Liquide,Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Appareil et procede de separation cryogenique d'un melange de monoxyde de carbone et de methane ainsi que d'hydrogene et/ou d'azote |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3596472A (en) * | 1967-12-20 | 1971-08-03 | Messer Griesheim Gmbh | Process for liquefying natural gas containing nitrogen |
US3721099A (en) * | 1969-03-25 | 1973-03-20 | Linde Ag | Fractional condensation of natural gas |
DE2502959A1 (de) * | 1975-01-24 | 1976-07-29 | Linde Ag | Verfahren zum verfluessigen von erdgas |
US4112700A (en) * | 1974-08-09 | 1978-09-12 | Linde Aktiengesellschaft | Liquefaction of natural gas |
DE3521060A1 (de) * | 1984-06-12 | 1985-12-12 | Snamprogetti S.P.A., Mailand/Milano | Verfahren zum kuehlen und verfluessigen von gasen |
US4680041A (en) * | 1985-12-30 | 1987-07-14 | Phillips Petroleum Company | Method for cooling normally gaseous material |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2297825A (en) * | 1995-02-03 | 1996-08-14 | Air Prod & Chem | Process to remove nitrogen from natural gas |
DE19716415C1 (de) * | 1997-04-18 | 1998-10-22 | Linde Ag | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
DE19920312A1 (de) * | 1999-05-03 | 2000-11-09 | Linde Ag | Verfahren und Vorrichtung zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
-
2001
- 2001-05-02 DE DE2001121339 patent/DE10121339A1/de not_active Withdrawn
-
2002
- 2002-04-29 AU AU2002319155A patent/AU2002319155B2/en not_active Ceased
- 2002-04-29 WO PCT/EP2002/004721 patent/WO2002088612A1/de active IP Right Grant
-
2003
- 2003-10-31 NO NO20034865A patent/NO20034865L/no not_active Application Discontinuation
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3596472A (en) * | 1967-12-20 | 1971-08-03 | Messer Griesheim Gmbh | Process for liquefying natural gas containing nitrogen |
US3721099A (en) * | 1969-03-25 | 1973-03-20 | Linde Ag | Fractional condensation of natural gas |
US4112700A (en) * | 1974-08-09 | 1978-09-12 | Linde Aktiengesellschaft | Liquefaction of natural gas |
DE2502959A1 (de) * | 1975-01-24 | 1976-07-29 | Linde Ag | Verfahren zum verfluessigen von erdgas |
DE3521060A1 (de) * | 1984-06-12 | 1985-12-12 | Snamprogetti S.P.A., Mailand/Milano | Verfahren zum kuehlen und verfluessigen von gasen |
US4680041A (en) * | 1985-12-30 | 1987-07-14 | Phillips Petroleum Company | Method for cooling normally gaseous material |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7520143B2 (en) | 2005-04-22 | 2009-04-21 | Air Products And Chemicals, Inc. | Dual stage nitrogen rejection from liquefied natural gas |
WO2010094396A3 (de) * | 2009-02-19 | 2013-04-18 | Linde Aktiengesellschaft | Verfahren zum abtrennen von stickstoff |
RU2537486C2 (ru) * | 2009-08-21 | 2015-01-10 | Линде Акциенгезелльшафт | Способ сжижения обогащенной углеводородами, содержащей азот сырьевой фракции, предпочтительно природного газа |
WO2014173598A3 (en) * | 2013-04-22 | 2015-12-03 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for producing a liquefied hydrocarbon stream |
Also Published As
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NO20034865D0 (no) | 2003-10-31 |
AU2002319155B2 (en) | 2007-03-29 |
DE10121339A1 (de) | 2002-11-07 |
NO20034865L (no) | 2003-10-31 |
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