AU2013200075B2 - Process for obtaining a pure helium fraction - Google Patents

Process for obtaining a pure helium fraction Download PDF

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AU2013200075B2
AU2013200075B2 AU2013200075A AU2013200075A AU2013200075B2 AU 2013200075 B2 AU2013200075 B2 AU 2013200075B2 AU 2013200075 A AU2013200075 A AU 2013200075A AU 2013200075 A AU2013200075 A AU 2013200075A AU 2013200075 B2 AU2013200075 B2 AU 2013200075B2
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fraction
helium
nitrogen
removal
compressed
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AU2013200075A1 (en
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Heinz Bauer
Andreas Bub
Martin Gwinner
Said Al Rabadi
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Linde GmbH
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Linde GmbH
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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
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J3/028—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 noble gases
    • F25J3/029—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 noble gases of helium
    • 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
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • 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
    • 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
    • F25J2215/30—Helium
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen

Abstract

Abstract Process for obtaining a pure helium fraction A process is described for obtaining a pure helium fraction from a starting fraction comprising at least helium, methane and nitrogen. According to the invention, a) the starting fraction (1) is subjected to an N2/CH4 removal (A), b) the fraction (2) which comprises essentially helium and nitrogen and is obtained in the N2/CH4 removal (A) is compressed (B), 10 c) the compressed fraction (3) is subjected to an N2 removal (D), and d) the helium-rich fraction (6) obtained in the N2 removal (D) is subjected to an adsorptive purification process (E) in which the pure helium fraction (7) is obtained. (This refers to Figure 2)

Description

COMPLETE SPECIFICATION
FOR A STANDARD PATENT
ORIGINAL
Name of Applicant:
Linde Aktiengesellschaft
Actual Inventors:
Heinz Bauer and Martin Gwinner and Andreas Bub and Said Al Rabadi
Address for Service is:
Shelston IP
60 Margaret Street Telephone No: (02) 9777 1111
SYDNEY NSW 2000 CCN: 3710000352 Attorney Code: SW Facsimile No. (02) 9241 4666
Invention Title: Process for obtaining a pure helium fraction
The following statement is a full description of this invention, including the best method of performing it known to me/us:File: 77456AUP00
2013200075 04 Jan 2013
Description
Process for obtaining a pure helium fraction
The invention relates to a process for obtaining a pure helium fraction from a starting fraction comprising at least helium, methane and nitrogen.
Helium is commercially obtained virtually exclusively from a mixture of volatile natural gas components, this mixture comprising, as well as helium, typically methane and nitrogen, and traces of hydrogen, argon and other noble gases. Helium collects with other gases in underground structures of sufficient gas-tightness. In the course of production of mineral oil, helium is made available as a component of the gas which accompanies the mineral oil, or in the course of production of natural gas. It is theoretically possible to obtain helium from the atmosphere, but this is uneconomic due to low concentrations.
In order to avoid unwanted freezing during a helium liquefaction process, the concentration of impurities in the helium stream to be liquefied must not exceed a value of 1000 ppmv, preferably 10 ppmv. For this reason, the helium liquefaction process is connected downstream of a helium purification process. The latter consists typically of a combination of cryogenic processes, generally based on partial condensation, and adsorptive processes, the regeneration in the case of the latter being possible through pressure and/or temperature swing.
In many cases, it is advantageous to design the helium purification process such that, as well as the purified helium, nitrogen of technical grade purity - wherein the sum of impurities is less than 100 ppmv, preferably less than 10 ppmv - can be obtained.
In order to be able to release nitrogen in the desired purity, however, an N2/CH4 separation additionally has to be provided. In general, only a portion, typically 5 to 70%, preferably 10 to 50%, of the nitrogen present in the mixture to be purified is brought to high purity. The remaining nitrogen is released to the atmosphere together with methane as a low-pressure gas, either directly or after an oxidation step, preferably implemented in a flare or an incinerator. If the methane content in this N2/CH4 fraction
2013200075 04 Jan 2013 is at least 10% by volume, it can also be released as fuel gas and/or be supplied to a methane recovery.
The working example shown in Figure 1 illustrates a generic process for obtaining a pure helium fraction from a starting fraction comprising at least helium, methane and nitrogen.
In this process, the starting fraction 100 is first subjected to a compression A’ to a pressure between 20 and 40 bar. The compressed starting fraction 101 is then, provided that it comprises hydrogen, subjected to a preferably catalytic hydrogen removal B’. The starting fraction 102 thus prepurified is then supplied to a cryogenic nitrogen removal C’. From this, an N2/CH4-rich fraction is drawn off via line 106 and is subjected to a cryogenic N2/CH4 removal E’. From this, an N2/CH4-rich fraction is drawn off via line 107 and a nitrogen fraction via line 108, the latter generally having a sum of impurities of less 100 ppmv, preferably less than 10 ppmv.
The helium-rich fraction 103 obtained in the cryogenic nitrogen removal C’ is subjected to an adsorptive purifying process D’. This process may be a TSA process, a PSA process, a VPSA process or a combination of the aforementioned processes. Via line
104, the pure helium fraction obtained therein is drawn off and supplied to the further use thereof, for example a liquefaction. The residual gas fraction 105 obtained in the adsorption process D’ can be added to the starting fraction 100.
It is an object of a preferred embodiment of the present invention to specify a generic process for obtaining a pure helium fraction which has lower capital and operating costs.
Any discussion of the prior art throughout the specification should in no way be considered as an admission that such prior art is widely known or forms part of common general knowledge in the field.
It is an object of the present invention to overcome or ameliorate at least one of the disadvantages of the prior art, or to provide a useful alternative.
2013200075 18 Oct 2017
To address this problem, a process is proposed for obtaining a pure helium fraction from a starting fraction comprising at least helium, methane and nitrogen, wherein
a) the starting fraction is subjected to an N2/CH4 removal,
b) the fraction which comprises essentially helium and nitrogen and is obtained in the
N2/CH4 removal is compressed,
c) the compressed fraction is subjected to an N2 removal, and
d) the helium-rich fraction obtained in the N2 removal is subjected to an adsorptive purification in which the pure helium fraction is obtained.
According to a first aspect of the invention there is provided a process for obtaining a pure helium fraction from a starting fraction comprising at least helium, methane and nitrogen, wherein the method comprises
a) subjecting the starting fraction to an N2/CH4 removal in a wash, to obtain a fraction comprising essentially heiium and nitrogen,
b) compressing the fraction which comprises essentially helium and nitrogen to obtain a compressed fraction,
c) subjecting the compressed fraction to an N2 removal to obtain a helium-rich fraction and a liquefied nitrogen flow,
d) subjecting the helium-rich fraction to an adsorptive purification process in which the pure helium fraction is obtained, and
e) supplying the liquefied nitrogen flow to the wash as reflux.
Unless the context clearly requires otherwise, throughout the description and the claims, the words “comprise”, “comprising”, and the like are to be construed in an inclusive sense as opposed to an exclusive or exhaustive sense; that is to say, in the sense of “including, but not limited to.
Further advantageous configurations of the process according to the invention for obtaining a pure heiium fraction, which are the subject matter of the dependent claims, are characterized in that
4a
2013200075 18 Oct 2017
- the compressed fraction is subjected to an H2 removal prior to supply to the N2 removal,
- the fraction which comprises essentially helium and nitrogen and is obtained in the N2/CH4 removal is compressed to a pressure between 15 and 35 bar, preferably between 20 and 25 bar,
- the adsorptive purifying process is designed as a TSA, PSA or VPSA process,
- the N2/CH4 removal is implemented by means of a wash, to which liquefied nitrogen which is obtained in the N2 removal is preferably supplied as reflux, and/or
- the wash is preferably operated at a pressure of 1.2 to 5 bar, preferably of 1.5 to
2 bar.
2013200075 04 Jan 2013
The process according to the invention for obtaining a pure helium fraction is explained in detail hereinafter with reference to the working example shown in Figure 2.
The starting fraction 1 comprising at least helium, methane and nitrogen is, in accordance with the invention, first subjected to an N2/CH4 removal A. The N2/CH4-rich fraction obtained is drawn off via line 10. The N2/CH4 removal A is preferably implemented by means of a wash or by a wash column. This is supplied with the starting fraction 1 at the bottom. Liquefied nitrogen (9) which is obtained in the N2 removal (D) yet to be described is preferably applied as reflux to the top of the wash column. The wash column is preferably operated at a pressure of 1.2 to 5 bar, especially of 1.5 to 2 bar. In addition, the wash column is operated at a temperature corresponding to the boiling temperature of nitrogen within the pressure range specified (-195 to -185°C).
The fraction 2 which comprises essentially helium and nitrogen and is obtained in the N2/CH4 removal A is subsequently supplied to a compression unit B. Compression is effected therein to a pressure between 15 and 35 bar, preferably between 20 and 25 bar.
If the starting fraction 1 or 2 comprises hydrogen, a preferably catalytic hydrogen removal unit C to which the compressed fraction 3 is supplied should be provided. The fraction 4 treated in the hydrogen removal unit C is then subjected to a preferably cryogenic nitrogen removal D. From this, a nitrogen-rich fraction is drawn off via line 5 and optionally supplied to the further use thereof, for example in helium precooling prior to liquefaction and in employment in the radiation shield of liquid helium tanks.
The helium-rich fraction 6 obtained in the nitrogen removal D is subjected to an adsorptive purifying process E, from which the pure helium fraction obtained is drawn off via line 7. In the case of the inventive process regime too, the residual gas fraction 8 obtained in the adsorptive purifying process E can be supplied to the starting fraction, in which case, however, it is now supplied to the fraction 2 which has already been substantially freed of methane and nitrogen.
In contrast to the procedure described with reference to Figure 1, in the case of the process according to the invention, a pure helium fraction is obtained by purifying the
2013200075 04 Jan 2013 starting fraction, prior to the compression thereof, to very substantially free it of methane, any further high boilers present and a majority of the nitrogen, typically 10 to 90%, preferably 30 to 80%. Only the remaining fraction comprising essentially helium and nitrogen is compressed to 15 to 35 bar, preferably 20 to 25 bar. In this case, a methane content of the compressed fraction of < 100 ppmv, preferably < 10 ppmv, is established.
The early removal of the N2/CH4 fraction reduces the burden on the downstream process steps. Even though two independent (cryogenic) removal steps are now 10 required, the capital and operating costs are lowered. Moreover, the further removal of combustible components considerably lowers the safety requirements (for example explosion protection) in the downstream process steps.
The nitrogen obtained in the N2 removal (D) fulfils the typical purity demands - this 15 means that the sum of impurities is <100 ppmv, preferably <10 ppmv - which are made on liquefied nitrogen which finds use in a helium plant. The liquefied nitrogen may find use, for example, in helium precooling prior to liquefaction and in employment in radiation shields of liquid helium tanks.

Claims (8)

  1. Claims
    2013200075 18 Oct 2017
    1. A process for obtaining a pure heiium fraction from a starting fraction comprising at least helium, methane and nitrogen, wherein the method comprises
    a) subjecting the starting fraction to an N2/CH4 removai in a wash, to obtain a
    5 fraction comprising essentially helium and nitrogen,
    b) compressing the fraction which comprises essentially helium and nitrogen to obtain a compressed fraction,
    c) subjecting the compressed fraction to an N2 removal to obtain a helium-rich fraction and a liquefied nitrogen flow,
    10 d) subjecting the helium-rich fraction to an adsorptive purification process in which the pure helium fraction is obtained, and
    e) supplying the liquefied nitrogen flow to the wash as reflux.
  2. 2. A process according to claim 1, wherein the compressed fraction is subjected to
    15 an Hi removai prior to supply to the N2 removal.
  3. 3. A process according to claim 1 or claim 2, wherein in step b) the fraction is compressed to a pressure between 15 and 35 bar.
    20
  4. 4. A process according to claim 3 wherein in step b) the fraction is compressed to a pressure between 20 and 25 bar.
  5. 5. A process according to any one of the preceding claims 1 to 4, wherein the adsorptive purifying process is a TSA, PSA or VPSA process.
  6. 6. A process according to any one of the preceding claims 1 to 5, wherein the wash is operated at a pressure of 1.2 to 5 bar.
  7. 7. A process according to claim 6, wherein the wash is operated at a pressure of 1.5
    30 to 2 bar.
  8. 8. A pure helium fraction obtained by the process according to any one of claims 1 to 7.
    1/1
    2013200075 04 Jan 2013
    Fig, 2
AU2013200075A 2012-01-05 2013-01-04 Process for obtaining a pure helium fraction Active AU2013200075B2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102012000147.9 2012-01-05
DE102012000147A DE102012000147A1 (en) 2012-01-05 2012-01-05 Method for obtaining a helium pure fraction

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AU2013200075A1 AU2013200075A1 (en) 2013-07-18
AU2013200075B2 true AU2013200075B2 (en) 2018-01-04

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Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3035656B1 (en) * 2015-04-30 2019-03-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude PRODUCTION OF HELIUM FROM A GASEOUS CURRENT CONTAINING HYDROGEN
US10962283B2 (en) 2018-09-13 2021-03-30 Air Products And Chemicals, Inc. Helium extraction from natural gas
FR3096900B1 (en) * 2019-06-06 2021-10-01 Air Liquide Helium purification process and unit

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006055324A2 (en) * 2004-11-19 2006-05-26 Praxair Technology, Inc. Light gas component separation

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4238211A (en) * 1978-11-20 1980-12-09 Helix Technology Corporation Method of employing a first contaminant to prevent freeze-out of a second contaminant during cryogenic processing of a gaseous stream
DE10106484A1 (en) * 2001-02-13 2002-08-14 Linde Ag Simultaneous recovery of helium and nitrogen pure fractions from process stream containing methane, nitrogen and helium, involves partially condensing process stream, and further processing
DE102005010054A1 (en) * 2005-03-04 2006-09-07 Linde Ag Process for simultaneously recovering a helium and a nitrogen pure fraction
DE102005010053A1 (en) * 2005-03-04 2006-09-07 Linde Ag Helium recovery in LNG plants

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006055324A2 (en) * 2004-11-19 2006-05-26 Praxair Technology, Inc. Light gas component separation

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RU2012157331A (en) 2014-07-10
RU2573083C2 (en) 2016-01-20
AU2013200075A1 (en) 2013-07-18

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