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GB2350417A - Fractionation of natural gas. - Google Patents

Fractionation of natural gas. Download PDF

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Publication number
GB2350417A
GB2350417A GB0010231A GB0010231A GB2350417A GB 2350417 A GB2350417 A GB 2350417A GB 0010231 A GB0010231 A GB 0010231A GB 0010231 A GB0010231 A GB 0010231A GB 2350417 A GB2350417 A GB 2350417A
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GB
United Kingdom
Prior art keywords
fraction
pure methane
producing
hydrocarbon
residual gas
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.)
Granted
Application number
GB0010231A
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GB2350417B (en
GB0010231D0 (en
Inventor
Rainer Sapper
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of GB0010231D0 publication Critical patent/GB0010231D0/en
Publication of GB2350417A publication Critical patent/GB2350417A/en
Application granted granted Critical
Publication of GB2350417B publication Critical patent/GB2350417B/en
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

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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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/09—Purification; Separation; Use of additives by fractional condensation
    • 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
    • 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
    • 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
    • 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
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/60—Methane
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • 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
    • 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

A pure methane fraction is produced by cryogenic fractionation of a hydrocarbon-rich fraction, for example natural gas, in which, in the cryogenic fractionation, in addition to a pure methane fraction, a residual gas fraction is produced and the fractionation takes place without provision of external refrigeration. The plant is arranged so that under partial load conditions a partial stream (8) of the pure methane fraction (4) and/or a partial stream (9) of the residual gas fraction (5) is recycled to a location upstream of the cryogenic fractionation stage (C). The amount of pure methane fraction (8) and/or residual gas fraction (9) recycled is sufficient to avoid the need for provision of external refrigeration. , Preferably, the hydrocarbon-rich fraction (1) to be fractionated is compressed (V) in a single stage or multiple stages and the partial stream (8) of the pure methane fraction (4) and/or of the partial stream (9) of the residual gas fraction (5) is fed upstream of the compression (V) or, in the case of a multistage compression, into one or more of the intermediate stages of the compression.

Description

2350417 PROCESS FOR PRODUCING A PURE METHANE FRACTION The present
invention relates to a process for producing a pure methane fraction by cryogenic fractionation of a hydrocarbon-rich fraction, for example natural gas, in which, in the cryogenic fractionation, in addition to a pure methane fraction, a residual gas fraction is produced and the fractionation takes place without provision of external refrigeration.
Processes of the generic type for producing a pure methane fraction by cryogenic fractionation of a hydrocarbon-rich fraction, for example natural gas, have long been known. Fractionations of this type do not require provision of external refrigeration if the cold box insulation losses occurring can be covered by "Joule-Thomson refrigeration". However, especially at relatively small pure methane flow rates - for example of the order of magnitude of up to 450 kg/h - under partial load operation there is the problem that the use of external refrigeration is needed if the desired product purities are to be maintained.
In addition, in plant of this type which is designed for such low pure methane flow rates, attention must be paid to the fact that the cold box, or the cryogenic fractionation columns provided therein, are designed for partial load operation. This means, for example, provision of correspondingly suitable column trays.
It is an object of the present invention to provide a process for producing a pure methane fraction by cryogenic fractionation of a hydrocarbon-rich fraction, which is successful even under partial load conditions without provision of external refrigeration, the product purities remaining substantially unchanged even under partial load operation and which ideally enables capital costs to be reduced.
According to the present invention there is provided a process for producing a pure methane fraction by cryogenic fractionation of a hydrocarbon-rich fraction in which, in the cryogenic fractionation, in addition to a pure methane fraction, a residual gas fraction is produced and the fractional takes place without provision of external refrigeration, wherein under partial load conditions a partial stream of the pure methane fraction and/or a partial stream of the residual gas fraction is recycled to a location upstream of the cryogenic 2 fractionation, with the amount of pure methane fraction and/or residual gas fraction recycled being sufficient to avoid the need for external refrigeration.
The hydrocarbon-rich fraction to be fractionated may be compressed, for example in a single stage or in multiple stages, upstream of the cryogenic fractionation stage and the partial stream of the pure methane fraction and/or the partial stream of the residual gas fraction may be fed to a location upstream of the compression stage or, in the case of a multiple stage compression, into an intermediate stage of the compression.
The hydrocarbon-rich fraction to be fractionated may be purified upstream of the cryogenic fractionation of components that might interfere in the cryogenic fractionation. The purification stage upstream of the cryogenic fractionation may comprise an adsorption stage and/or a scrubbing stage. A partial stream of the residual gas fraction may be fed to the adsorption stage as regeneration gas.
The hydrocarbon-rich fraction may comprise natural gas.
For a better understanding of the present invention and to show more clearly how it may be carried into effect reference will now be made, by way of example, to the accompanying figure which illustrates one method by which the present invention may be put into effect.
A hydrocarbon-rich fraction, for example, natural gas, essentially consisting of methane (2: 80% by volume), nitrogen (from 10 to 15% by volume), higher hydrocarbons and, if appropriate, carbon dioxide, is fed via line 1 to a compression unit V. In the compression unit, which can be of single-stage or multistage design, the hydrocarbon-rich fraction is compressed to a pressure for example from 25 to 35 bar. For the sake of clarity, in the figure the coolers and separators provided downstream of the individual compression stages are not shown.
The compressed hydrocarbon-rich fraction is fed via line 2 to a purification unit P. In the purification unit P the hydrocarbon-rich fraction is dried and all those components which are unwanted for subsequent process stages or which could adversely affect subsequent process stages are removed. Thus, for example, the removal of carbon dioxide is absolutely necessary, since otherwise this would freeze in the downstream cryogenic fractionation and lead to deposits in the lines and valves.
3 The compressed and purified hydrocarbon-rich fraction is fed via line 3 to the cryogenic fractionator C, which is shown only as a black (cold) box in the figure for the sake at clarity. A conventional cryogenic fractionation is carried out, for example in two rectification columns, in which case the higher hydrocarbons are taken off from the bottom of the first rectification column while a nitrogen-rich fraction is produced at the top of the second rectification column. These two residual gas fractions can then be taken off either separately or together from the cryogenic fractionator C.
In a process procedure of this type, a pure methane fraction is produced from the bottom of the second rectification column, and is similarly removed from the cryogenic fractionator C. In the present case, the pure methane fraction is taken off via line 4 from the cold box, while the combined residual gas fractions are taken off from the cold box C via line 5. Conventional purity requirements for the pure methane fraction to be produced require a degree of methane purity of at least 99.9% by volume.
If the purification unit P is designed as a pressure-swing (pressure change) adsorption process, a partial stream 6 of the residual gas fraction 5 can be fed to the adsorption process for the purpose of regeneration. The loaded regeneration gas leaves the adsorption process P via a line 7 and, if appropriate, is fed to further use.
In addition, or alternatively, to a pressure-swing adsorption process, a scrubber can be provided, by means of which all those components which are unwanted for subsequent process stages or could adversely affect subsequent process stages can be removed.
According to the invention, when operating under partial load conditions, at least one partial stream 8 of the pure methane fraction 4 and/or at least one partial stream 9 of the residual gas fraction 5 is recycled to a location upstream of the cryogenic fractionator C.
According to an advantageous embodiment of the process according to the invention, these streams are recycled to a location upstream of the compression stage V or, in the case of a multistage compression, to one or more of the intermediate stages of the compressor.
4 In order to be able to control the flow rate of recycled pure methane fraction 8 and/or recycled residual gas fraction 9, two control valves a and b are provided. The valves a and b are actuated by means of appropriate flow controllers (FC's).
The recycling of at least one partial stream 8 of the pure methane fraction 4 and/or of at least one partial stream 9 of the residual gas fraction 5 to a location upstream of the cryogenic fractionator then makes it possible for the process for producing a pure methane fraction to be able to proceed even when operating under the partial load, under the same conditions as when operating under full load. This means that the cryogenic fractionator C (and the cold box) is always under a constant load even when the process as a whole is operating under partial load conditions.
The process can therefore be operated at all times under optimal boundary conditions, as present under full load operation. Thus, even under partial load operation no change in product purity of the pure methane fraction occurs. According to the invention, then, even in the partial load operation, the provision of external refrigeration can be avoided.
It is also not required for the cryogenic fractionator C (or cold box) to be designed for partial load operation, as has been required previously, which results in a decrease in capital cost compared with known process procedures.

Claims (11)

1. A process for producing a pure methane fraction by cryogenic fractionation of a hydrocarbon-rich fraction in which, in the cryogenic fractionation, in addition to a pure methane fraction, a residual gas fraction is produced and the fractionation takes place without provision of external refrigeration, wherein under partial load conditions a partial stream of the pure methane fraction and/or a partial stream of the residual gas fraction is recycled to a location upstream of the cryogenic fractionation, with the amount of pure methane fraction and/or residual gas fraction recycled being sufficient to avoid the need for external refrigeration.
2. A process for producing a pure methane fraction according to claim 1, wherein the hydrocarbon-rich fraction to be fractionated is compressed upstream of the cryogenic fractionation stage and the partial stream of the pure methane fraction and/or the partial stream of the residual gas fraction is fed to a location upstream of the compression.
3. A process for producing a pure methane fraction according to claim 2, wherein the hydrocarbon-rich fraction is compressed in a single stage.
4. A process for producing a pure methane fraction according to claim 3, wherein the hydrocarbon-rich fraction is compressed in multiple stages.
5. A process for producing a pure methane fraction according to claim 4, wherein the partial stream of the pure methane fraction and/or the partial stream of the residual gas fraction is fed to an intermediate compression stage.
6. A process for producing a pure methane fraction according to any preceding claim, wherein the hydrocarbon-rich fraction to be fractionated is purified upstream of the cryogenic fractionation of components that might interfere with the cryogenic fractionation.
7. A process for producing a pure methane fraction according to claim 6, wherein the purification stage upstream of the cryogenic fractionation comprises an adsorption stage.
6
8. A process for producing a pure methane fraction according to claim 7, wherein a partial stream of the residual gas fraction is fed to the adsorption stage as regeneration gas.
9. A process for producing a pure methane fraction according to claim 6, 7 or 8, wherein the purification stage upstream of the cryogenic fractionation comprises a scrubbing stage.
10. A process for producing a pure methane fraction according to any preceding claim, wherein the hydrocarbon-rich fraction comprises natural gas.
11. A process for producing a pure methane fraction by cryogenic fractionation of a hydrocarbon-rich fraction substantially as hereinbefore described with reference to the accompanying drawing.
GB0010231A 1999-04-30 2000-04-28 Process for producing a pure methane fraction Expired - Fee Related GB2350417B (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE19919932A DE19919932A1 (en) 1999-04-30 1999-04-30 Process for obtaining a pure methane fraction

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GB0010231D0 GB0010231D0 (en) 2000-06-14
GB2350417A true GB2350417A (en) 2000-11-29
GB2350417B GB2350417B (en) 2003-04-09

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120017640A1 (en) * 2009-02-19 2012-01-26 Linde Aktiengesellschaft Process for separating off nitrogen
US8435403B2 (en) 2009-02-10 2013-05-07 Linde Aktiengesellschaft Process for removing nitrogen

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2904869B1 (en) * 2006-08-09 2008-11-07 Air Liquide UNIT AND METHOD FOR DEAZATING NATURAL GAS
DE102015001858A1 (en) * 2015-02-12 2016-08-18 Linde Aktiengesellschaft Combined separation of heavy and light ends from natural gas
EP3885312B1 (en) * 2020-03-26 2022-12-14 L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude Process and plant for producing pure carbon monoxide and hydrogen
FR3110223A1 (en) * 2020-05-15 2021-11-19 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for extracting nitrogen from a stream of natural gas or bio-methane

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1204076A (en) * 1967-12-27 1970-09-03 Messer Griesheim Gmbh Process for the liquifaction of hydrocarbon gas mixtures
US4451275A (en) * 1982-05-27 1984-05-29 Air Products And Chemicals, Inc. Nitrogen rejection from natural gas with CO2 and variable N2 content
US5351491A (en) * 1992-03-31 1994-10-04 Linde Aktiengesellschaft Process for obtaining high-purity hydrogen and high-purity carbon monoxide
WO1998050742A1 (en) * 1997-05-07 1998-11-12 Elcor Corporation Process for separating hydrocarbon gas constituents

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4237620A1 (en) * 1992-11-06 1994-05-11 Linde Ag Process for the production of high-purity liquid methane

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1204076A (en) * 1967-12-27 1970-09-03 Messer Griesheim Gmbh Process for the liquifaction of hydrocarbon gas mixtures
US4451275A (en) * 1982-05-27 1984-05-29 Air Products And Chemicals, Inc. Nitrogen rejection from natural gas with CO2 and variable N2 content
US5351491A (en) * 1992-03-31 1994-10-04 Linde Aktiengesellschaft Process for obtaining high-purity hydrogen and high-purity carbon monoxide
WO1998050742A1 (en) * 1997-05-07 1998-11-12 Elcor Corporation Process for separating hydrocarbon gas constituents

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8435403B2 (en) 2009-02-10 2013-05-07 Linde Aktiengesellschaft Process for removing nitrogen
US20120017640A1 (en) * 2009-02-19 2012-01-26 Linde Aktiengesellschaft Process for separating off nitrogen

Also Published As

Publication number Publication date
GB2350417B (en) 2003-04-09
DE19919932A1 (en) 2000-11-02
NL1015065A1 (en) 2000-10-31
NL1015065C2 (en) 2001-05-08
GB0010231D0 (en) 2000-06-14

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