AU2010230576A1 - Method for liquefying a hydrocarbon-rich fraction - Google Patents
Method for liquefying a hydrocarbon-rich fraction Download PDFInfo
- Publication number
- AU2010230576A1 AU2010230576A1 AU2010230576A AU2010230576A AU2010230576A1 AU 2010230576 A1 AU2010230576 A1 AU 2010230576A1 AU 2010230576 A AU2010230576 A AU 2010230576A AU 2010230576 A AU2010230576 A AU 2010230576A AU 2010230576 A1 AU2010230576 A1 AU 2010230576A1
- Authority
- AU
- Australia
- Prior art keywords
- fraction
- cooled
- temperature level
- hydrocarbon
- liquid fraction
- 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
Links
- 238000000034 method Methods 0.000 title claims abstract description 36
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 25
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 25
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 37
- 239000003507 refrigerant Substances 0.000 claims abstract description 30
- 230000006835 compression Effects 0.000 claims abstract description 21
- 238000007906 compression Methods 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 abstract description 5
- 239000000203 mixture Substances 0.000 abstract 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000012080 ambient air Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 230000005514 two-phase flow Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000012432 intermediate storage Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000010943 off-gassing Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
-
- 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
Landscapes
- 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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A method for liquefying a hydrocarbon-rich fraction is described, wherein the cooling and liquefaction of the hydrocarbon-rich fraction is implemented by indirect heat exchange with the refrigerant mixture of a refrigerant mixture circuit, the refrigerant mixture is compressed at least in a two-stage manner and is separated into a gaseous and a liquid fraction after each compression stage, wherein the gaseous fraction of the final compression stage is cooled to the lowest temperature level, while the liquid fraction of the intermediate compression stages or at least one of the intermediate compression stages is cooled to a temperature level lying above the lowest temperature level. According to the invention, the liquid fraction (3), which is cooled to a temperature level lying above the lowest temperature level, is cooled (E3) prior to the indirect heat exchange (E) with the hydrocarbon-rich fraction (20) to be liquefied.
Description
1 Description Process for liquefyinq a hydrocarbon-rich fraction The invention relates to a process for liquefying a hydrocarbon-rich fraction, wherein the hydrocarbon-rich fraction is cooled and liquefied in indirect heat exchange against 5 the mixed refrigerant of a mixed refrigerant cycle, the mixed refrigerant is compressed in at least two stages and after each compression stage is separated into a gaseous fraction and a liquid fraction, wherein the gaseous fraction of the last compression stage is cooled to the lowest temperature level, while the liquid fraction of the intermediate compression stages, or at least one of the intermediate compression 10 stages, is cooled to a temperature level above the lowest temperature level. In natural gas liquefaction processes having production rates of 30 000 to 3 million tons/year of LNG, mixed refrigerant cycles having only one cycle compressor are frequently used, these are also termed single mixed refrigerant (SMR) processes. 15 A generic method for liquefying a hydrocarbon-rich fraction will be described in more detail hereinafter with reference to the liquefaction process shown in Figure 1. The cycle compressor required for this liquefaction process has two compression 20 stages V1 and V2. The mixed refrigerant compressed in the first compression stage V1 - customarily a compression proceeds to 10 to 40 bar, preferably 15 to 25 bar - is partially condensed in the aftercooler or heat exchanger El, preferably against ambient air or water, and fed via line 1 to a separator D1. In this it is separated into a gaseous fraction and also a liquid fraction. The gaseous fraction is fed via line 2 to the second 25 compressor stage V2 and in this compressed to the desired final pressure which is customarily between 25 and 80 bar, preferably between 30 and 50 bar. An aftercooler E2 in which the compressed refrigerant fraction is cooled preferably against ambient air or water is also arranged downstream of the second compression 30 stage V2. Via line 4, this refrigerant fraction is subsequently fed to a further separator D2. The gaseous refrigerant fraction taken off at the top of the separator D2 via line 5 is fed 2 to the main heat exchanger E, cooled in this against process streams which are to be warmed, and taken off at the cold end of the heat exchanger E via line 7. The heat exchanger E is preferably constructed as a multistream heat exchanger, in particular as a plate heat exchanger or helically coiled heat exchanger. 5 Via line 20, the hydrocarbon-rich fraction which is to be liquefied and is, for example, a natural gas stream, is fed to the heat exchanger E. After liquefaction has been performed, the liquefied product stream is taken off from the heat exchanger E via line 21 and fed to its further use or an intermediate storage. 10 The refrigerant fraction taken off from the heat exchanger E via line 7 is cold producingly expanded in the valve a and fed via the line 8 through the heat exchanger E in countercurrent to the hydrocarbon-rich fraction 20 which is to be cooled and to be liquefied. Via the pipe sections 8 and 8', this refrigerant fraction is subsequently fed to 15 the first compression stage V1. The liquid fraction taken off from the bottom phase of the separator D1 via line 3 is, after cooling in the heat exchanger E, taken off therefrom via line 9, cold-producingly expanded in the valve b and subsequently passed through the heat exchanger E via 20 line 10 in countercurrent to the hydrocarbon-rich fraction which is to be cooled and to be liquefied. Subsequently, this refrigerant fraction is mixed with the abovedescribed refrigerant fraction in the line 8 and fed together with it via line 8' to the first compression stage V1. 25 The liquid fraction occurring in the bottom phase of the second separator D2 is cold producingly expanded in the valve c to the pressure of the first separator D1 and is recirculated upstream thereof. The liquid refrigerant fraction taken off from the separator D1 via line 3 is customarily in 30 the boiling state. A boiling refrigerant liquid, however, generally suffers from a pressure drop due to friction and/or to an ascending pipe arrangement. This pressure drop inevitably leads to partial outgassing of light components of this refrigerant fraction. Therefore unwanted formation of a two-phase flow occurs. This can lead to unstable flow conditions in the pipes and/or to distribution faults - these are taken to mean 35 uneven fractions of gas and liquid in parallel flow paths, for example of heat 3 exchangers - in the downstream apparatuses. It is an object of the present invention to specify a process of the type in question for liquefying a hydrocarbon-rich fraction, which process avoids the abovementioned disadvantages. 5 This object is achieved by a proposed process for liquefying a hydrocarbon-rich fraction, which is characterized in that the liquid fraction which is cooled to a temperature level above the lowest temperature level is cooled upstream of the indirect heat exchange with the hydrocarbon-rich fraction which is to be liquefied. 10 Owing to the cooling or subcooling to be provided according to the invention of the liquid refrigerant fraction, the formation of a two-phase stream and the disadvantages associated therewith can be effectively avoided. 15 Other advantageous configurations of the process according to the invention for liquefying a hydrocarbon-rich fraction which are subjects of the dependent claims are characterized in that - the liquid fraction which is cooled to a higher temperature level is cooled 20 upstream of the indirect heat exchange with the hydrocarbon-rich fraction to be liquefied to a temperature which is between 2 and 150C, preferably between 4 and 7*C, below the temperature which the compressed mixed refrigerant has during the separation into a gaseous fraction and a liquid fraction, 25 - the liquid fraction which is cooled to a higher temperature level is cooled in indirect heat exchange against the or a boiling fraction which originates from the separation into a gaseous fraction and a liquid fraction which is connected downstream of a subsequent compression stage, 30 - the heat exchange between the hydrocarbon-rich fraction to be liquefied and the mixed refrigerant proceeds in a multistream heat exchanger which is preferably constructed as a plate heat exchanger or helically coiled heat exchanger, and 35 - at least occasionally, at least one substream of the fraction which is cooled to 4 the lowest temperature level is expanded and mixed with the expanded liquid fraction of the fraction which is cooled to a temperature level which is above the lowest temperature level. 5 The process according to the invention for liquefying a hydrocarbon-rich fraction and also further configurations of the same will be described in more detail hereinafter with reference to the exemplary embodiment shown in Figure 2. In the description of the exemplary embodiment shown in Figure 2, hereinafter only the differences from the process procedure shown in Figure 1 will be considered. 10 According to the invention, now a heat exchanger E3 is provided which enables a heat exchange between the two liquid fractions taken off from the separators D1 and D2 via the lines 3 and 6. Since the liquid fraction taken off from the separator D2 via line 6 is expanded in the valve c to the pressure of the separator D1, the liquid fraction cools by 15 partial evaporation to a temperature which is below the process temperature achievable in the aftercoolers El and E2. The liquid fraction cooled in this manner which is present in the line 6 downstream of the valve c now cools or subcools in the heat exchanger E3 the liquid fraction which is taken off from the separator D1 via line 3. 20 In this case the liquid fraction 3 is cooled or subcooled by 2 to 150C, preferably by 4 to 70C, below the process temperature achievable in the aftercoolers El and E2. The liquid fraction which is cooled in this manner and taken off from the separator D1 25 via line 3 can now be fed to the heat exchanger E and conducted through it without the disadvantageous effects described at the outset occurring. The heat exchanger E3 is preferably constructed as a countercurrent heat exchanger, for example as a linear tube exchanger. Advantageously, in practice the heat 30 exchanger E3 is arranged in such a manner that it is arranged below the valve c and above the separator D1. This gradient between valve c, heat exchanger E3 and separator D1 leads to the two-phase flow of the stream 6 being kept stable after expansion in the valve c. 35 In a development of the process according to the invention for liquefying a 5 hydrocarbon-rich fraction, it is proposed to expand at least occasionally at least one substream of the fraction which is cooled to the lowest temperature level, and to add it to the expanded liquid fraction of the fraction which is cooled to a temperature level above the lowest temperature level. Such a process procedure is achieved, for 5 example, in that, via the lines 11 and/or 12, mixed refrigerant substreams are taken off at the cold end of the heat exchanger E or at a suitable intermediate temperature, expanded in the valve d or e and are added to the expanded liquid fraction 9. A suitable intermediate temperature is present when the refrigerant fraction 5 has a subcooling of at least 5*C, preferably at least 100C, compared with the boiling state. In 10 practice, in most cases either valve d or e will be provided. Such a process procedure enables the control of the temperature or temperature profile in the heat exchanger E to be improved. The embodiment shown in Figure 2, owing to the integration of subcooling of the liquid 15 fraction 3 into the compression V1/V2 achieved therein, has the advantage that a temperature of the liquid fraction 3 can be achieved before the feed into the heat exchanger E, which temperature is below the temperature which would be achievable in the case of cooling against ambient air or cooling water without requiring an additional cooling for this by a separate refrigeration plant and/or by another cold 20 process stream. The procedure shown in Figure 2 enables the wanted separation between the subcooling of the refrigerant 3 achieved in heat exchanger E3 and the operation of other plant components. This separation is of importance, in particular in the startup of 25 the liquefaction process, since cold process streams customarily are not available until after the start up of the process, and therefore cannot be used from the start for subcooling. The process according to the invention for liquefying a hydrocarbon-rich fraction 30 enables, with low increased structural expenditure - only one additional heat exchanger E3 must be provided - the elimination of the problems described at the outset as occur in the liquefaction processes included as part of the prior art.
Claims (5)
1. Process for liquefying a hydrocarbon-rich fraction, wherein the hydrocarbon-rich fraction is cooled and liquefied in indirect heat exchange against the mixed refrigerant of a mixed refrigerant cycle, the mixed refrigerant is compressed in at 5 least two stages and after each compression stage is separated into a gaseous fraction and a liquid fraction, wherein the gaseous fraction of the last compression stage is cooled to the lowest temperature level, while the liquid fraction of the intermediate compression stages, or at least one of the intermediate compression stages, is cooled to a temperature level above the lowest temperature level, 10 characterized in that the liquid fraction (3) which is cooled to a temperature level above the lowest temperature level is cooled (E3) upstream of the indirect heat exchange (E) with the hydrocarbon-rich fraction (20) which is to be liquefied.
2. Process according to Claim 1, characterized in that the liquid fraction (3) which is 15 cooled to a higher temperature level is cooled (E3) upstream of the indirect heat exchange (E) with the hydrocarbon-rich fraction (20) to be liquefied to a temperature which is between 2 and 15*C, preferably between 4 and 7C, below the temperature which the compressed mixed refrigerant has during the separation (D1) into a gaseous fraction and a liquid fraction. 20
3. Process according to Claim 1 or 2, characterized in that the liquid fraction (3) which is cooled to a higher temperature level is cooled (E3) in indirect heat exchange against the or a boiling fraction (6) which originates from the separation (D2) into a gaseous fraction and a liquid fraction which is connected downstream 25 of a subsequent compression stage (V2).
4. Process according to any one of the preceding Claims 1 to 3, characterized in that the heat exchange between the hydrocarbon-rich fraction (20) to be liquefied and the mixed refrigerant (3, 5, 7, 9) proceeds in a multistream heat exchanger (E) 30 which is preferably constructed as a plate heat exchanger or helically coiled heat exchanger.
5. Process according to any one of the preceding Claims 1 to 4, characterized in that at least occasionally, at least one substream (11, 12) of the fraction (5, 7) which is u I.u'j uuJ - %uI:>rupiu uLd[IuUug 7 cooled (E) to the lowest temperature level is expanded (d, e) and mixed with the expanded liquid fraction of the fraction (9) which is cooled (E) to a temperature level which is above the lowest temperature level.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102009016046A DE102009016046A1 (en) | 2009-04-02 | 2009-04-02 | Process for liquefying a hydrocarbon-rich fraction |
| DE102009016046.9 | 2009-04-02 | ||
| PCT/EP2010/002034 WO2010112206A2 (en) | 2009-04-02 | 2010-03-30 | Method for liquefying a hydrocarbon-rich fraction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU2010230576A1 true AU2010230576A1 (en) | 2011-09-15 |
| AU2010230576B2 AU2010230576B2 (en) | 2016-02-18 |
Family
ID=42675003
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2010230576A Ceased AU2010230576B2 (en) | 2009-04-02 | 2010-03-30 | Method for liquefying a hydrocarbon-rich fraction |
Country Status (11)
| Country | Link |
|---|---|
| CN (1) | CN102575896B (en) |
| AR (1) | AR076136A1 (en) |
| AU (1) | AU2010230576B2 (en) |
| BR (1) | BRPI1013386A2 (en) |
| CL (1) | CL2011002391A1 (en) |
| DE (1) | DE102009016046A1 (en) |
| MY (1) | MY161644A (en) |
| NO (1) | NO20111413A1 (en) |
| PE (1) | PE20120848A1 (en) |
| RU (1) | RU2538156C2 (en) |
| WO (1) | WO2010112206A2 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102011010633A1 (en) * | 2011-02-08 | 2012-08-09 | Linde Ag | Method for cooling a one-component or multi-component stream |
| DE102014018412A1 (en) * | 2014-12-09 | 2016-06-09 | Linde Aktiengesellschaft | Flare-free starting of a natural gas liquefaction process |
| DE102015004125A1 (en) * | 2015-03-31 | 2016-10-06 | Linde Aktiengesellschaft | Process for liquefying a hydrocarbon-rich fraction |
| US10323880B2 (en) | 2016-09-27 | 2019-06-18 | Air Products And Chemicals, Inc. | Mixed refrigerant cooling process and system |
| US10753676B2 (en) | 2017-09-28 | 2020-08-25 | Air Products And Chemicals, Inc. | Multiple pressure mixed refrigerant cooling process |
| US10852059B2 (en) * | 2017-09-28 | 2020-12-01 | Air Products And Chemicals, Inc. | Multiple pressure mixed refrigerant cooling system |
Family Cites Families (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4325231A (en) * | 1976-06-23 | 1982-04-20 | Heinrich Krieger | Cascade cooling arrangement |
| FR2540612A1 (en) * | 1983-02-08 | 1984-08-10 | Air Liquide | METHOD AND INSTALLATION FOR COOLING A FLUID, IN PARTICULAR A LIQUEFACTION OF NATURAL GAS |
| US4525185A (en) * | 1983-10-25 | 1985-06-25 | Air Products And Chemicals, Inc. | Dual mixed refrigerant natural gas liquefaction with staged compression |
| DE19722490C1 (en) * | 1997-05-28 | 1998-07-02 | Linde Ag | Single flow liquefaction of hydrocarbon-rich stream especially natural gas with reduced energy consumption |
| GB9712304D0 (en) * | 1997-06-12 | 1997-08-13 | Costain Oil Gas & Process Limi | Refrigeration cycle using a mixed refrigerant |
| GB2326464B (en) * | 1997-06-12 | 2001-06-06 | Costain Oil Gas & Process Ltd | Refrigeration cycle using a mixed refrigerant |
| US6347531B1 (en) * | 1999-10-12 | 2002-02-19 | Air Products And Chemicals, Inc. | Single mixed refrigerant gas liquefaction process |
| US6347532B1 (en) * | 1999-10-12 | 2002-02-19 | Air Products And Chemicals, Inc. | Gas liquefaction process with partial condensation of mixed refrigerant at intermediate temperatures |
| US6742357B1 (en) * | 2003-03-18 | 2004-06-01 | Air Products And Chemicals, Inc. | Integrated multiple-loop refrigeration process for gas liquefaction |
| US20080173043A1 (en) * | 2005-03-09 | 2008-07-24 | Sander Kaart | Method For the Liquefaction of a Hydrocarbon-Rich Stream |
| CN201417042Y (en) * | 2009-04-27 | 2010-03-03 | 赵德泉 | Equipment with simplified mixed refrigerant liquefaction process |
-
2009
- 2009-04-02 DE DE102009016046A patent/DE102009016046A1/en not_active Withdrawn
-
2010
- 2010-03-18 AR ARP100100874A patent/AR076136A1/en not_active Application Discontinuation
- 2010-03-30 AU AU2010230576A patent/AU2010230576B2/en not_active Ceased
- 2010-03-30 WO PCT/EP2010/002034 patent/WO2010112206A2/en not_active Ceased
- 2010-03-30 PE PE2011001669A patent/PE20120848A1/en not_active Application Discontinuation
- 2010-03-30 CN CN201080015211.2A patent/CN102575896B/en not_active Expired - Fee Related
- 2010-03-30 MY MYPI2011004663A patent/MY161644A/en unknown
- 2010-03-30 RU RU2011144360/06A patent/RU2538156C2/en not_active IP Right Cessation
- 2010-03-30 BR BRPI1013386A patent/BRPI1013386A2/en not_active Application Discontinuation
-
2011
- 2011-09-27 CL CL2011002391A patent/CL2011002391A1/en unknown
- 2011-10-18 NO NO20111413A patent/NO20111413A1/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| NO20111413A1 (en) | 2011-10-18 |
| MY161644A (en) | 2017-04-28 |
| AU2010230576B2 (en) | 2016-02-18 |
| BRPI1013386A2 (en) | 2016-03-29 |
| CN102575896A (en) | 2012-07-11 |
| RU2538156C2 (en) | 2015-01-10 |
| CL2011002391A1 (en) | 2012-02-10 |
| WO2010112206A3 (en) | 2012-10-11 |
| AR076136A1 (en) | 2011-05-18 |
| WO2010112206A2 (en) | 2010-10-07 |
| CN102575896B (en) | 2015-04-22 |
| DE102009016046A1 (en) | 2010-10-07 |
| PE20120848A1 (en) | 2012-07-11 |
| RU2011144360A (en) | 2013-05-10 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FGA | Letters patent sealed or granted (standard patent) | ||
| MK14 | Patent ceased section 143(a) (annual fees not paid) or expired |