AU2009200347B2 - Process for obtaining helium - Google Patents
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- AU2009200347B2 AU2009200347B2 AU2009200347A AU2009200347A AU2009200347B2 AU 2009200347 B2 AU2009200347 B2 AU 2009200347B2 AU 2009200347 A AU2009200347 A AU 2009200347A AU 2009200347 A AU2009200347 A AU 2009200347A AU 2009200347 B2 AU2009200347 B2 AU 2009200347B2
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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
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
- F25J3/061—Natural gas or substitute 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/066—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/0685—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of noble gases
- F25J3/069—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of noble gases of helium
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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
- 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
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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
- 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
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—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
- F25J2270/00—Refrigeration techniques used
- F25J2270/08—Internal refrigeration by flash gas recovery 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Abstract Process for obtaining helium A process is described for separating off helium from a helium-containing fraction, in particular from a helium-, nitrogen- and methane-containing fraction. According to the invention a) the helium-containing fraction (5) is at least in part condensed (E2) and divided (D2) into a helium-enriched gas fraction (6) and a helium depleted liquid fraction (9'), b) the helium-enriched gas fraction (6) is condensed (E3) at least until the helium concentration in the resultant gas fraction (7) is at least 90%, preferably at least 95%, and in particular at least 98%, c) the helium-depleted liquid fraction (9') is expanded (b'), vaporized until at least 70%, preferably at least 85%, of the helium contained therein is in the gaseous state and divided (D4) into a helium-rich gas fraction (11') and a helium-poor liquid fraction (12') and d) the helium-rich gas fraction (11') is warmed and added to the helium-containing fraction (5). (Figure 2 is associated herewith).
Description
- 1 AUSTRALIA PATENTS ACT 1990 COMPLETE SPECIFICATION FOR A STANDARD PATENT ORIGINAL Name of Applicant/s: Linde Aktiengesellschaft Actual Inventor/s: Hans Schmidt Address for Service is: SHELSTON IP 60 Margaret Street Telephone No: (02) 9777 1111 SYDNEY NSW 2000 Facsimile No. (02) 9241 4666 CCN: 3710000352 Attorney Code: SW Invention Title: PROCESS FOR OBTAINING HELIUM The following statement is a full description of this invention, including the best method of performing it known to me/us: File: 61449AUP00 - la PROCESS FOR OBTAINING HELIUM The invention relates to a process for separating off helium from a helium-containing fraction, in particular from a helium-, nitrogen- and methane-containing fraction. 5 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. Natural gas generally contains low fractions of helium; 10 these fractions are conventionally between 0.1 and 0.5%. During the liquefaction of the natural gas the helium accumulates in what is termed the residual gas. This residual gas is therefore the most frequent source for obtaining helium. A further source of a helium-containing 15 fraction is the intermediate expansion of LNG (Liquefied Natural Gas). A prior art process for separating off helium from a helium-rich fraction may be explained in more detail with reference to the example shown in Figure 1. 20 Line 1, a helium-containing fraction which has a helium fraction between 1 and 10%, is fed to a compressor C1. This helium-containing fraction is, for example, the residual gas from an LNG tank. The helium-containing fraction is compressed to a pressure between 2 and 10 bar, 25 cooled in the heat exchanger El and condensed until the helium in the remaining gas fraction is concentrated to concentrations > 10%. The helium-containing fraction is condensed in the heat exchanger El against a refrigerant stream conducted via 30 line 3' through the heat exchanger El, which refrigerant stream is preferably a nitrogen stream. From the bottom of the separator D1, via line 3, a nitrogen-rich fraction is taken off, expanded in the -2 valve a to the pressure prevailing in the line 3' and fed to the above described refrigerant stream. The helium-containing fraction taken off at the top of 5 the separator Dl via line 4 is warmed to ambient temperature in the heat exchanger El and subsequently compressed in the compressor C2 to a pressure between 15 and 40 bar. 10 Via line 5, the compressed fraction is fed to a possibly necessary prepurification A which serves for removing hydrogen, carbon monoxide and/or carbon dioxide and/or drying, and subsequently cooled in heat exchanger E2 and in this process condensed until the 15 helium concentration in the gas phase is greater than 70%. The helium-enriched gas fraction which is taken off from the separator D2a via line 6 is condensed in the heat exchanger E3 until the helium concentration in the gas phase is greater than 98%. The helium 20 concentration of the gas fraction which is taken off via line 7 at the top of the separator D3 enables complete liquefaction of this fraction in a helium liquefaction plant which is not shown in the figure, but, if appropriate, the remaining trace components 25 such as, for example, oxygen, hydrogen, carbon monoxide, carbon dioxide, argon, neon, nitrogen etc. must be further separated off. From the bottom of the separator D3, via line 8, a 30 helium-poor liquid fraction is taken off, expanded so as to produce cold in the valve e, warmed in the heat exchangers E3 and E2 against process streams which are to be cooled and taken off from the plant via line 8' In the above described valve e, an expansion preferably 35 proceeds to a pressure between 100 and 300 mbara, wherein the pressure is maintained by a vacuum pump P arranged at the warm end.
- 3 Should the amount of the liquid fraction which is taken off via line 8 not be sufficient to cover the cold requirement in the heat exchangers E2 and E3, if 5 appropriate, a refrigerant, for example in the form of external nitrogen, can be added via line 16 or 16'. The helium-depleted liquid fraction which is taken off from the bottom of the separator D2a via line 9 still 10 contains significant fractions of helium. By means of at least two separators D2b and D2c connected downstream of the separator D2a, this helium is separated off from the liquid fraction which is taken off via line 9. The separators D2b, D2c, ... operate in 15 this case at different pressures in order to restrict the temperature difference in the heat exchanger E2. The liquid fraction from the bottom of the separator D2a, before it is fed into the separator D2b, is 20 expanded (valve b). The same applies to the liquid fraction which is taken off from the bottom of the separator D2b via line 11, which liquid fraction is likewise expanded (valve c) before entry into the separator D2c. The gas fractions produced in the 25 separators D2b and D2c are recirculated via the pipe sections 10 and 10' and also after warming in the heat exchanger E2 to the helium-containing ~ fraction 4 upstream of the second compressor C2. As a result it is possible likewise to obtain the helium contained in 30 these gas fractions. Depending on the pressure of the gas fraction in the line 10', this gas fraction is added to the helium containing fraction via line 15 upstream of the first 35 compressor C1, or via line 10' upstream of the second compressor C2.
- 4 The liquid fractions which are taken off from the abovementioned separators D2b and D2c are used to cover the cold requirement in the heat exchanger E2. For this they are vaporized at ambient temperature and subsequently given 5 off. If there is an additional cold requirement, a suitable refrigerant, preferably nitrogen, is added via line 14. The above described process for obtaining helium is relatively intensive in terms of apparatus. Nevertheless, 10 the helium contained in the feed gas cannot be obtained completely, since a small helium fraction remains in the liquid fractions which are taken off from the separators D1, D2b and D2c and these are not used for obtaining helium. Furthermore, the helium is obtained from the 15 separator chain D2a to D2c at a low pressure and therefore must be recirculated upstream of the second compressor C2. However, an unwanted high expenditure on compression results therefrom. It is an object of the present invention to overcome or 20 ameliorate at least one of the disadvantages of the prior art, or to provide a useful alternative. The present invention relates to a process of the type in question for separating off helium from a helium-containing fraction, in particular from a helium-, nitrogen- and 25 methane-containing fraction, which process avoids the abovementioned disadvantages. 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 30 inclusive sense as opposed to an exclusive or exhaustive sense; that is to say, in the sense of "including, but not limited to".
- 4a Although the invention will be described with reference to specific examples it will be appreciated by those skilled in the art that the invention may be embodied in many other forms. 5 According to a first aspect, the present invention provides a process for separating off helium from a helium containing fraction, wherein a) the helium-containing fraction is at least in part condensed and divided into a helium-enriched gas 10 fraction and a helium-depleted liquid fraction, b) the helium-enriched gas fraction is condensed at least until the helium concentration in the resultant gas fraction is at least 90%, c) the helium-depleted liquid fraction is expanded, 15 vaporized until at least 70%, of the helium contained therein is in the gaseous state and divided into a helium-rich gas fraction and a helium-poor liquid fraction and d) the helium-rich gas fraction is warmed and added to 20 the helium-containing fraction. According to a second aspect, the present invention provides helium produced by a process according to the first aspect. Further advantageous embodiments of the process according 25 to the invention for separating off helium from a helium containing fraction are characterized in that - the helium-containing fraction, before its condensation and division into a helium-enriched gas fraction and a helium-depleted liquid fraction is 30 compressed in a single stage or multistage manner, preferably to a pressure of between 10 and SO bar, - the helium-containing fraction, before its condensation and division into a helium-enriched gas - 5 fraction and a helium-depleted liquid fraction, is subjected to nitrogen separation, - the nitrogen-rich fraction produced in the nitrogen separation is expanded to a lower pressure, is divided into 5 a helium-containing, nitrogen-depleted gas fraction and a nitrogen-enriched liquid fraction, the helium-containing, nitrogen-depleted gas fraction is warmed and fed to the helium-containing fraction, preferably upstream of the compression thereof, -6 - the nitrogen-rich fraction produced in the nitrogen separation, after its expansion and before its division into a helium-containing 5 nitrogen-depleted gas fraction and a nitrogen enriched liquid fraction, is at least in part vaporized, - an external refrigerant, preferably nitrogen, is 10 provided for support of the condensation of the helium-containing fraction, the helium-enriched gas fraction and/or the helium-depleted liquid fraction, 15 - the helium-containing fraction, preferably after its compression, is purified from interfering components, in particular from hydrogen, carbon monoxide, carbon dioxide and/or water and 20 - the helium-rich gas fraction which is added to the helium-containing fraction, in accordance with its pressure is fed upstream or into the compression of the helium-containing fraction. 25 The process according to the invention for separating off helium from a helium-containing fraction and also further embodiments of the same will be described in more detail hereinafter with reference to exemplary embodiments illustrated in Figures 2 and 3. 30 In the exemplary embodiment shown in Figure 2, the process operation up to division of the helium containing fraction 5 in the separators D2 and D3 is identical to the procedure described with reference to 35 Figure 1, for which reason repetition will be avoided and instead reference is made to the corresponding sections of the description of Figure 1.
-7 According to the invention the separator chain explained with reference to Figure 1, represented by the separators D2b and. D2c - in practice, as mentioned, 5 three or more series-arranged separators can also be implemented -, is now replaced according to the invention by a single separator D4. The helium-enriched gas fraction which is taken off at 10 the top of the separator D2 via line 6 is condensed in the heat exchanger E3 until the helium concentration in the gas fraction obtained in the downstream separator D3, which is fed via line 7 to a helium liquefaction process, is at least 90%, preferably at least 95%, and 15 in particular at least 98%. In order nevertheless to be able to obtain the helium from the liquid fraction which is taken off from the separator D2 and in this process not to exceed the 20 maximum permissible temperature difference in the heat exchanger E2, the helium-depleted liquid fraction which is taken off from the separator D2 via line 9' is first expanded in valve b to a corresponding pressure and subsequently vaporized in the heat exchanger E2 until 25 the majority of the helium dissolved therein converts to the gas phase. This is taken to mean that this liquid fraction is vaporized until at least 70%, preferably at least 85%, of the helium contained therein is present in the gas state. 30 The helium-rich gas fraction which is taken off at the top of the separator D4 via line 11' is warmed in the heat exchanger E2 to ambient temperature and depending on the pressure level of the preceding 35 expansion in the valve b - fed via the lines 11' or 11'' upstream or into the compressor C2.
- 8 From the bottom of the separator D4, via the line 12', a virtually helium-free liquid fraction is taken off, expanded in the valve c', warmed to ambient temperature in the heat exchanger E2 and subsequently taken off via 5 line 13'. Should this liquid fraction not be able to cover the cold requirement of the heat exchanger E2, refrigerant, preferably nitrogen, can be fed via line 14'. The abovementioned liquid fraction which is taken off via line 13' is either fed to its further 10 use, for example as regeneration gas for the prepurification unit A operating by adsorption, or is given off to the atmosphere. An advantageous embodiment of the process according to 15 the invention is shown in Figure 3, in which the nitrogen-rich fraction which is produced during the nitrogen separation in the bottom of the separator D1 and is taken off via line 3 is subjected to a helium separation. 20 For this, the nitrogen-rich fraction which is taken off via line 3 is expanded in valve a, at least in part vaporized in the heat exchanger El and subsequently separated in separator D'. The above described 25 (partial) vaporization can also be omitted. Advantageously, the expansion a proceeds to a pressure which permits this fraction to be given off to the atmosphere after warming in the heat exchanger El. 30 In the separator Dl' mentioned, separation into a helium-containing nitrogen-depleted gas fraction and a nitrogen-enriched liquid fraction proceeds. Whereas the latter fraction, after warming in the heat exchanger El is taken off - should it not be able to cover the cold 35 requirement of the heat exchanger El, additional refrigerant can be fed via line 23 - the helium- -9 containing, nitrogen-depleted gas fraction is fed via line 21 to the helium-containing fraction in line 1. This advantageous embodiment of the process according 5 to the invention enables the helium to be obtained to the greatest possible extent from the nitrogen-rich fraction obtained in the nitrogen separation. The process according to the invention for separating 10 off helium from a helium-containing fraction, in particular from a helium-, nitrogen- and methane containing fraction, has a plurality of advantages compared with the prior art processes, which advantages are listed hereinafter: 15 - saving at least one apparatus (separator) in what is termed the cold part of the helium separation - increasing the helium yield to greater than 99.8%; 20 known processes enable helium yields only up to 99.3% - saving compression energy, since the fraction still containing residual amounts of helium which 25 is recirculated to the feed fraction upstream of the compression is produced at a higher pressure than in the prior art processes; therefore feed into the compressor C2 at an intermediate pressure is possible 30 - decreasing the recycle stream upstream of the compressor Cl which in turn leads to a reduction of the energy consumption of the overall process 35 - the heat exchanger E2 can be constructed without large thermal stresses, since temperature - 10 differences which are to be maintained as a maximum can be maintained without problems - the nitrogen content in the fraction fed to the 5 helium liquefaction process is lowered, from which lower expenditure on separating off the nitrogen upstream of the final helium liquefaction results.
Claims (20)
1. Process for separating off helium from a helium containing fraction, wherein a) the helium-containing fraction is at least in part 5 condensed and divided into a helium-enriched gas fraction and a helium-depleted liquid fraction, b) the helium-enriched gas fraction is condensed at least until the helium concentration in the resultant gas fraction is at least 90%, 10 c) the helium-depleted liquid fraction is expanded, vaporized until at least 70%, of the helium contained therein is in the gaseous state and divided into a helium-rich gas fraction and a helium-poor liquid fraction and 15 d) the helium-rich gas fraction is warmed and added to the helium-containing fraction.
2. Process according to claim 1 wherein the helium containing fraction is a helium-, nitrogen- and methane containing fraction. 20
3. Process according to claim 1 or claim 2 wherein the helium-enriched gas fraction is condensed at least until the helium concentration in the resultant gas fraction is at least 95%.
4. Process according to claim 3 wherein the helium 25 enriched gas fraction is condensed at least until the helium concentration in the resultant gas fraction is at least 98%.
5. Process according to any one of the preceding claims wherein the helium-depleted liquid fraction is expanded, 30 vaporized until at least 85% of the helium contained therein is in the gaseous state and divided into a helium rich gas fraction and a helium-poor liquid fraction. - 12
6. Process according to any one of the preceding claims, wherein the helium-containing fraction, before its condensation and division into a helium-enriched gas fraction and a helium-depleted liquid fraction is 5 compressed in a single stage or multistage manner.
7. Process according to claim 6, wherein the helium containing fraction, before its condensation and division into a helium-enriched gas fraction and a helium-depleted liquid fraction is compressed in a single stage or 10 multistage manner, to a pressure of between 10 and 50 bar.
8. Process according to any one of the preceding claims, wherein the helium-containing fraction, before its condensation and division into a helium-enriched gas fraction and a helium-depleted liquid fraction, is 15 subjected to nitrogen separation.
9. Process according to claim 8, wherein the nitrogen rich fraction produced in the nitrogen separation is expanded (a) to a lower pressure, is divided into a helium containing, nitrogen-depleted gas fraction, and a nitrogen 20 enriched gas fraction, the helium-containing, nitrogen depleted gas fraction is warmed and fed to the helium containing fraction.
10. Process according to claim 9, wherein the helium containing, nitrogen-depleted gas fraction is warmed and 25 fed to the helium-containing fraction, upstream of the compression thereof.
11. Process according to claim 9 or claim 10, wherein the nitrogen-rich fraction produced in the nitrogen separation, after its expansion (a) and before its division into a 30 helium-containing nitrogen-depleted gas fraction and a nitrogen-enriched liquid fraction, is at least in part vaporized.
12. Process according to any one of the preceding claims, wherein an external refrigerant is provided for support of - 13 the condensation of the helium-containing fraction, the helium-enriched gas fraction and/or the helium-depleted liquid fraction.
13. Process according to claim 12, wherein the external 5 refrigerant is nitrogen.
14. Process according to any one of the preceding claims, wherein the helium-containing fraction is purified (A) from interfering components.
15. Process according to claim 14, wherein the helium 10 containing fraction is purified (A) after its compression.
16. Process according to claim 14 or claim 15, wherein the interfering components are selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide and/or water. 15
17. Process according to any one of the preceding claims, wherein the helium-rich gas fraction which is added to the helium-containing fraction, in accordance with its pressure is fed upstream or into the compression of the helium containing fraction. 20
18. Helium produced by a process according to any one of the preceding claims.
19. Process for separating off helium from a helium containing fraction, said process substantially as herein described with reference to any one of the accompanying 25 drawings and/or examples but excluding comparative examples.
20. Helium produced by a process, said process substantially as herein described with reference to any one of the accompanying drawings and/or examples but excluding 30 comparative examples.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102008007925A DE102008007925A1 (en) | 2008-02-07 | 2008-02-07 | Separating helium, comprises condensing helium-containing fraction, separating into e.g. helium-enriched gas fraction, condensing the gas fraction, evaporating liquid fraction, separating into e.g. helium-rich gas fraction and heating |
| DE102008007925.1 | 2008-02-07 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU2009200347A1 AU2009200347A1 (en) | 2009-08-27 |
| AU2009200347B2 true AU2009200347B2 (en) | 2013-08-22 |
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ID=40847232
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2009200347A Ceased AU2009200347B2 (en) | 2008-02-07 | 2009-01-30 | Process for obtaining helium |
Country Status (3)
| Country | Link |
|---|---|
| AU (1) | AU2009200347B2 (en) |
| DE (1) | DE102008007925A1 (en) |
| RU (1) | RU2486131C2 (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102008022208A1 (en) | 2008-05-06 | 2009-11-12 | Linde Ag | Treating a gas stream containing nitrogen and methane, comprises subjecting the gas stream to regenerative thermal oxidation process, which makes the methane depletion |
| DE102011115984A1 (en) | 2011-10-14 | 2013-04-18 | Linde Ag | Separation of helium from helium-containing methane realms fraction involves separating helium-containing methane-rich fraction, methane-enriched fraction and helium-enriched fraction, compressing, separating, purifying and cleaning |
| DE102012008446A1 (en) | 2012-04-26 | 2013-10-31 | Linde Aktiengesellschaft | Method for obtaining pure helium-fraction from helium-containing, methane- and nitrogen-rich feed fraction, involves condensing feed fraction at ten bar pressure, which is separated into helium-depleted fraction and helium-rich fraction |
| US10036590B2 (en) | 2012-08-02 | 2018-07-31 | Air Products And Chemicals, Inc. | Helium recovery from streams containing helium, carbon dioxide, and at least one of nitrogen and methane |
| US9791210B2 (en) | 2012-08-02 | 2017-10-17 | Air Products And Chemicals, Inc. | Systems and methods for recovering helium from feed streams containing carbon dioxide |
| RU2578144C1 (en) * | 2014-10-24 | 2016-03-20 | Александр Евгеньевич Угроватов | Method for production of ultrapure compressed helium in cylinders |
| DE102014018883A1 (en) * | 2014-12-17 | 2016-06-23 | Linde Aktiengesellschaft | Combined membrane pressure swing adsorption process for the recovery of helium |
| DE102015001664A1 (en) * | 2015-02-10 | 2016-08-11 | Linde Aktiengesellschaft | Helium recovery process |
| CA2984085C (en) | 2016-11-01 | 2019-04-09 | Jason Michael Ploeger | Helium recovery from streams containing helium, carbon dioxide, and at least one of nitrogen and methane |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4758258A (en) * | 1987-05-06 | 1988-07-19 | Kerr-Mcgee Corporation | Process for recovering helium from a natural gas stream |
| DE3716898A1 (en) * | 1987-05-20 | 1988-12-15 | Bergwerksverband Gmbh | METHOD AND DEVICE FOR HELIUM ENHANCEMENT |
| DE4100933A1 (en) * | 1991-01-15 | 1992-07-16 | Achenbach Cryotechnik Gmbh | Helium purificn. plant using inert diatomaceous earth adsorber filters - for safer operation in presence of liquid oxygen@ residues |
| MY114649A (en) * | 1998-10-22 | 2002-11-30 | Exxon Production Research Co | A process for separating a multi-component pressurized feed stream using distillation |
| FR2832213B1 (en) * | 2001-11-12 | 2004-09-24 | Air Liquide | PROCESS AND PLANT FOR THE PRODUCTION OF HELIUM |
-
2008
- 2008-02-07 DE DE102008007925A patent/DE102008007925A1/en not_active Ceased
-
2009
- 2009-01-30 AU AU2009200347A patent/AU2009200347B2/en not_active Ceased
- 2009-02-06 RU RU2009104099/05A patent/RU2486131C2/en not_active IP Right Cessation
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2009200347A1 (en) | 2009-08-27 |
| RU2009104099A (en) | 2010-08-20 |
| DE102008007925A1 (en) | 2009-08-13 |
| RU2486131C2 (en) | 2013-06-27 |
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