MX2010009024A - Metodo para separar nitrogeno de gas natural. - Google Patents
Metodo para separar nitrogeno de gas natural.Info
- Publication number
- MX2010009024A MX2010009024A MX2010009024A MX2010009024A MX2010009024A MX 2010009024 A MX2010009024 A MX 2010009024A MX 2010009024 A MX2010009024 A MX 2010009024A MX 2010009024 A MX2010009024 A MX 2010009024A MX 2010009024 A MX2010009024 A MX 2010009024A
- Authority
- MX
- Mexico
- Prior art keywords
- fraction
- nitrogen
- rich
- hydrocarbon
- initial
- Prior art date
Links
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 21
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title abstract description 13
- 239000003345 natural gas Substances 0.000 title abstract description 4
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 19
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 19
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 claims description 2
- 238000001179 sorption measurement Methods 0.000 claims description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 claims 1
- 229910052739 hydrogen Inorganic materials 0.000 claims 1
- 238000010899 nucleation Methods 0.000 claims 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 abstract 1
- 238000001816 cooling Methods 0.000 description 7
- 239000003949 liquefied natural gas Substances 0.000 description 7
- 239000002737 fuel gas Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 150000002500 ions Chemical class 0.000 description 3
- 239000003990 capacitor Substances 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002829 nitrogen Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—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
- F25J1/0211—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0219—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—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
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- 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
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- F25J2270/00—Refrigeration techniques used
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- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
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- Separation By Low-Temperature Treatments (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Se describe un método para licuar una fracción inicial rica en hidrocarburo que contiene nitrógeno, preferiblemente gas natural. De conformidad con la invención a) la fracción inicial se licua, b) se separa mediante rectificación en una fracción enriquecida del nitrógeno cuyo contenido de metano es de máximo 1% en volumen, y una fracción rica en hidrocarburo, empobrecida de nitrógeno, c) la fracción rica en hidrocarburo, empobrecida de nitrógeno se subfusiona y se expande, d) la fracción rica en hidrocarburo, empobrecida de nitrógeno expandida se desdobla en una fracción líquida rica en hidrocarburo cuyo contenido de nitrógeno es de máximo 1% en volumen y una fracción rica en nitrógeno, y e) la fracción rica en nitrógeno se mezcla con la fracción inicial.
Description
METODO PARA SEPARAR NITROGENO DE GAS NATURAL
DESCRIPCION DE LA INVENCION
La invención se refiere a un método para li ión inicial rica en hidrocarburo que contiene ni riblemente de gas natural.
Las fracciones iniciales o respectivament ales ricos en hidrocarburo que contienen n eren de medidas adecuadas para licuarlas, par ar la concentración de nitrógeno en el produc (gas natural licuado) a 1% en volumen. En el cas concentración de nitrógeno, dentro del ta enamiento del GNL se producen estratifi eables y peligrosas en virtud de las di dades . Para evitar esto, el nitrógeno usualm sa del proceso extrayendo una flujo de gas com enden turbinas de gas que pueden usar al almente el flujo de gas combustible precede onado. Sin embargo, en este caso es necesari do de que la máxima concentración de nitrógeno a flujo de gas combustible se encuentre entre 20 en. En cuanto el contenido de nitrógeno de la al a ser licuada es tan alto que no es posible l contenido de nitrógeno máximo admisible en el y en el flujo de gas combustible precede onado usualmente se extrae del proceso de licu fracción de nitrógeno altamente concentrad nido de metano es inferior a 1% en volume ión de nitrógeno altamente concentrado se pued tamente a la atmósfera. La generación de esta nitrógeno se puede efectuar o bien media blamiento del flujo de gas combustible en lo facción.
Una fracción inicial rica en hidrocarb ene nitrógeno se alimenta mediante la línea 1 so de licuefacción representado por los cambia o zonas El a E3 del cambiador de calor. La cir dibujada a rayas constituye en este caso un pr geración cualquiera o bien una planta de refrí uiera que se puede usar, por ejemplo, en la licu subenfriamiento de la fracción inicial mencionad
En el cambiador de calor o bien en la zon iador de calor tiene lugar primero un enfriamien ión inicial, la cual a continuación se alimenta ínea 102 a un segundo cambiador de calor o bien eí cambiador de calor y en esta se licúa por c ante la línea 103 y la válvula a de expansión la ial ahora licuada se alimenta a una columna De se macenamiento de GNL no representado en la figura
De la cabeza de la columna De separació e mediante la línea 108 una fracción de n ente concentrado; su contenido de nitrógeno us cuentra entre 90 y 100% en volumen. Una parte ión de nitrógeno se emite directamente a la a nte la línea 109, en tanto que otro flujo pa fracción de nitrógeno se alimenta mediante la l flujo de retorno a la columna De separación TI ber pasado por el condensador E4 de retorno disp parador DI .
Sin embargo, una forma de proceder como l ibe mediante la figura 1 provoca problemas si n io para el flujo 107 de gas combustible, el cu emitir directamente a la atmósfera, contrariame sucede con fracción 109 de nitrógeno a Para solucionar este problema se especi o para licuar una fracción inicial rica en hidr ontiene nitrógeno en el cual
a) la fracción inicial se licúa,
b) mediante rectificación se separa ión enriquecida de nitrógeno cuyo contenido má o es de 1% en volumen y una fracción carburo, empobrecida de nitrógeno,
c) la fracción rica en hidrocarburo, emp trógeno se subfusiona y se expande,
d) la fracción rica en hidrocarburo ex recida de nitrógeno se separa en una fracción en hidrocarburo cuyo contenido de nitrógeno es en como máximo y una fracción rica en nitrógeno, e) la fracción rica en nitrógeno se mezcl ión inicial .
ión inicial,
si la fracción inicial se somete a un ecado por adsorción previo a su enfriamie teriza porque la fracción rica en nitrógeno se gas regenerador para el proceso de secado por a de mezclarla con la fracción inicial,
un flujo parcial de la fracción ada se alimenta como gas extractor (stripgas e en inglés) a la subsiguiente separaci ficación de la fracción inicial licuada,
la licuefacción y/o el subenfriamient ión inicial rica en hidrocarburo que contiene n fectúa utilizando cualquier proceso de licuef eción,
si la fracción rica en hidrocarburo contenido de nitrógeno es de máximo 1% en vo nte la conducción del proceso representado en l ora el flujo de gas combustible que se produce proceso de licuefacción y tras la expansión ión inicial licuada y superfría ya no se alimen io de gas combustible como, por ejemplo, una tu sino que se mezcla con la fracción inicial a ser de alimentarla al proceso de enfriami facción .
El método de conformidad con la invenci r una fracción inicial rica en hidrocarburo que geno así como los perfeccionamientos adiciona se explicarán con más detalle a continuación emplo de realización representado en la figura 2.
De manera análoga a la forma de proceder figura 1, la fracción inicial rica en hidrocar ene nitrógeno se alimenta mediante las líneas 1 diante lo cual se apoya el efecto de rectificaci na de separación TI.
Del sumidero de la columna de separació e mediante la línea 4 una fracción rica en hidro recida de nitrógeno y se subfusiona en el camb o bien en la zona E3 del cambiador de calor.
La circulación 20 dibujada en líneas senta un proceso de refrigeración cualquiera o a de refrigeración cualquiera, como se puede u lo, en la licuefacción y subfusión de la al mencionada.
Esta fracción superfría se extrae del pr facción propiamente dicho mediante la línea 5, se válvula b y se alimenta a un separador DI. Med 6 se extrae del sumidero del separador DI una fra cto GNL licuada y se alimenta a un ta pasado a través del condensador de retorno E4 d separador DI .
Convenientemente el condensador de retorno ador DI se colocan tan altos que el retorno 11 ina de separación TI se puede efectuar mediante f dad sin el uso de una bomba. Además, la presió ador DI es de al menos 2 bara, preferiblemente permitir una transferencia sin bombeo de la fra cto GNL a un tanque de almacenamiento férico .
De acuerdo con un perfeccionamiento favor o de conformidad con la invención es posible qu eños un flujo parcial de la fracción 10 enriqu geno para el enfriamiento previo de la fra al antes de emitirlo a la atmósfera. Sí la fr al se somete a un proceso de secado como se de este propósito el gas perdido por ebullición de lmacenamiento de GNL atmosférico convenientem ime primero a la presión del separador D nuación a la presión de la fracción 1 inicial j acción 7 rica en nitrógeno extraída del separado
La fracción rica en nitrógeno o bien fra ombustible que se extrae de la cabeza del sepa nte la línea 7 ahora se comprime Cl de conform nvención en una o varias etapas, se enfría ador adicional E5 y a continuación se mezcla med 8 con la fracción inicial rica en hidrocar ene nitrógeno de la línea 1. Si la fracción 1 in ntra presente con una presión comparativamente le mezclar la fracción 7 rica en nitrógeno pri acción 1 inicial y luego someterla junto con el esión.
nte la figura 1 se producen tres fracciones dife ión de producto GNL, fracción de gas combus ión de nitrógeno altamente concentrado - que se proceso, en el caso del método de conformidad ción son únicamente dos fracciones, especifíca ión 6 del producto GNL así como la fracción geno altamente concentrado que se extrae de la c lumna de separación TI.
El retorno de la fracción 7 rica en nitróg ión 1 inicial tiene por consecuencia de que al licuefacción favorablemente se le sobrepo lación mixta indefinida. Esta circulación inida consta esencialmente de los componentes n tano así como pequeñas cantidades de hidro iores y eventualmente oxígeno y trazas de hel lación mixta indefinida se preenfría en el camb na de separación TI y se alimentan nuevament ión 1 inicial con la fase gaseosa del separador D
En combinación con el proceso de refriger la planta 20 de refrigeración que puede comprend técnicas conocidas como, por ejemplo, evapora cto puro, evaporación mixta, expansión de ctor de trabajo así como cualesquiera combinac resulta una cascada de circulación refrigerante lación mixta N2/CH4 indefinida en el extremo f so de licuefacción.
Mediante la formación de la circulació inida es posible proporcionar al condensador de el enfriamiento requerido independientemente sición y la presión de la fracción inicial, d a cantidad total del nitrógeno contenido en la al se puede reconcentrar a la pureza requerida
Claims (1)
- REIVINDICACIONES Habiéndose descrito la invención como ante ma como propiedad lo contenido en las si ndicaciones : 1. Método para licuar una fracción inici idrocarburo que contiene nitrógeno, preferiblen natural, caracterizado porque a) la fracción in , b) se desdobla mediante rectificación en una uecida de nitrógeno cuyo contenido máximo de m % en volumen y una fracción rica en hidro recida de nitrógeno, c) la fracción r carburo, empobrecida de nitrógeno se subfusió de, d) la fracción rica en hidrocarburo, empobr geno expandida se desdobla en una fracción líqu idrocarburo cuyo contenido máximo de nitrógeno ndicaciones 1 ó 2 en el cual la fracción ini e a un proceso de secado por adsorción a arla, caracterizado porque la fracción rica en n sa como gas regenerador para el proceso de se ción antes de mezclarla con la fracción inicial. 4. Método de conformidad con cualquiera ndicaciones 1 a 3 precedentes, caracterizado p parcial de la fracción inicial enfriada se gas extractor al subsiguiente desdoblamie ficación de la fracción inicial licuada. 5. Método de conformidad con cualquiera ndicaciones 1 a 4 precedentes, caracterizado p facción y/o la subfusión de la fracción inicial carburo que contiene nitrógeno se efectúa ut uier proceso de licuefacción a discreción. 6. Método de conformidad con cualquiera
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DE102009038458A DE102009038458A1 (de) | 2009-08-21 | 2009-08-21 | Verfahren zum Abtrennen von Stickstoff aus Erdgas |
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CN (1) | CN101993749A (es) |
AU (1) | AU2010202992A1 (es) |
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EP2457046A2 (en) * | 2009-07-21 | 2012-05-30 | Shell Internationale Research Maatschappij B.V. | Method for treating a multi-phase hydrocarbon stream and an apparatus therefor |
DE102011010633A1 (de) | 2011-02-08 | 2012-08-09 | Linde Ag | Verfahren zum Abkühlen eines ein- oder mehrkomponentigen Stromes |
AU2012354774B2 (en) * | 2011-12-12 | 2015-09-10 | Shell Internationale Research Maatschappij B. V. | Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition |
US9816754B2 (en) * | 2014-04-24 | 2017-11-14 | Air Products And Chemicals, Inc. | Integrated nitrogen removal in the production of liquefied natural gas using dedicated reinjection circuit |
US9945604B2 (en) | 2014-04-24 | 2018-04-17 | Air Products And Chemicals, Inc. | Integrated nitrogen removal in the production of liquefied natural gas using refrigerated heat pump |
US20150308737A1 (en) | 2014-04-24 | 2015-10-29 | Air Products And Chemicals, Inc. | Integrated Nitrogen Removal in the Production of Liquefied Natural Gas Using Intermediate Feed Gas Separation |
CN108144320A (zh) * | 2017-12-23 | 2018-06-12 | 天津市鹏翔科技有限公司 | 特殊精馏自平衡分相无泵回流控制方法 |
US11221176B2 (en) * | 2018-08-14 | 2022-01-11 | Air Products And Chemicals, Inc. | Natural gas liquefaction with integrated nitrogen removal |
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FR2682964B1 (fr) * | 1991-10-23 | 1994-08-05 | Elf Aquitaine | Procede de deazotation d'un melange liquefie d'hydrocarbures consistant principalement en methane. |
FR2714722B1 (fr) * | 1993-12-30 | 1997-11-21 | Inst Francais Du Petrole | Procédé et appareil de liquéfaction d'un gaz naturel. |
DE4440406C1 (de) * | 1994-11-11 | 1996-04-04 | Linde Ag | Verfahren zum Verflüssigen einer unter Druck stehenden kohlenwasserstoffreichen Fraktion |
GB2298034B (en) * | 1995-02-10 | 1998-06-24 | Air Prod & Chem | Dual column process to remove nitrogen from natural gas |
DZ2535A1 (fr) * | 1997-06-20 | 2003-01-08 | Exxon Production Research Co | Procédé perfectionné pour la liquéfaction de gaz naturel. |
DE10121339A1 (de) * | 2001-05-02 | 2002-11-07 | Linde Ag | Verfahren zum Abtrennen von Stickstoff aus einer Stickstoff-entaltenden Kohlenwasserstoff Fraktion |
UA76750C2 (uk) * | 2001-06-08 | 2006-09-15 | Елккорп | Спосіб зрідження природного газу (варіанти) |
US6658892B2 (en) * | 2002-01-30 | 2003-12-09 | Exxonmobil Upstream Research Company | Processes and systems for liquefying natural gas |
US6978638B2 (en) * | 2003-05-22 | 2005-12-27 | Air Products And Chemicals, Inc. | Nitrogen rejection from condensed natural gas |
DE102004049694A1 (de) * | 2004-10-12 | 2006-04-13 | Linde Ag | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
EP1715267A1 (en) * | 2005-04-22 | 2006-10-25 | Air Products And Chemicals, Inc. | Dual stage nitrogen rejection from liquefied natural gas |
JP2008169244A (ja) * | 2007-01-09 | 2008-07-24 | Jgc Corp | 天然ガス処理方法 |
DE102007010032A1 (de) * | 2007-03-01 | 2008-09-04 | Linde Ag | Verfahren zum Abtrennen von Stickstoff aus verflüssigtem Erdgas |
US20080216511A1 (en) * | 2007-03-09 | 2008-09-11 | Henry Edward Howard | Nitrogen production method and apparatus |
GB2455462B (en) * | 2009-03-25 | 2010-01-06 | Costain Oil Gas & Process Ltd | Process and apparatus for separation of hydrocarbons and nitrogen |
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RU2537486C2 (ru) | 2015-01-10 |
NO20101164A1 (no) | 2012-02-22 |
US20110041389A1 (en) | 2011-02-24 |
RU2010135055A (ru) | 2012-02-27 |
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