AU2006222325B2 - Method for liquefaction of a stream rich in hydrocarbons - Google Patents
Method for liquefaction of a stream rich in hydrocarbons Download PDFInfo
- Publication number
- AU2006222325B2 AU2006222325B2 AU2006222325A AU2006222325A AU2006222325B2 AU 2006222325 B2 AU2006222325 B2 AU 2006222325B2 AU 2006222325 A AU2006222325 A AU 2006222325A AU 2006222325 A AU2006222325 A AU 2006222325A AU 2006222325 B2 AU2006222325 B2 AU 2006222325B2
- Authority
- AU
- Australia
- Prior art keywords
- fraction
- refrigerant
- stream
- liquefaction
- lower boiling
- 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.)
- Ceased
Links
- 238000000034 method Methods 0.000 title claims description 36
- 229930195733 hydrocarbon Natural products 0.000 title claims description 33
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 33
- 239000003507 refrigerant Substances 0.000 claims description 47
- 238000009835 boiling Methods 0.000 claims description 42
- 239000000203 mixture Substances 0.000 claims description 27
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 24
- 239000004215 Carbon black (E152) Substances 0.000 claims description 21
- 230000006835 compression Effects 0.000 claims description 13
- 238000007906 compression Methods 0.000 claims description 13
- 239000003345 natural gas Substances 0.000 claims description 11
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 5
- 239000000470 constituent Substances 0.000 claims description 4
- 239000001294 propane Substances 0.000 claims description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims 1
- 238000001816 cooling Methods 0.000 description 7
- 238000000926 separation method Methods 0.000 description 2
- 239000002826 coolant Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- -1 natural gas Chemical class 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 230000001052 transient effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- F25J1/02—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
- 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
- F25J1/003—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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
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)
Description
Translation from German of PCT Application PCT/EP2006/001804 Method for liquefaction of a stream rich in hydrocarbons 5 The invention relates to a method for liquefaction of a stream rich in hydrocarbons, particularly a natural gas stream. 10 Natural gas liquefaction plants are designed either as so-called LNG baseload plants - i.e. plants for the liquefaction of natural gas for the supply of natural gas as a primary energy source - or as so-called peak shaving plants - i.e. plants for the liquefaction of natural gas 15 to cover peak demand. Larger LNG plants are generally operated with cooling circuits consisting of hydrocarbon mixtures. These mixture circuits are energetically more efficient than 20 expander circuits and enable relatively low specific energy consumptions. From DE-A 102 09 799 there is a method known for the liquefaction of a stream rich in hydrocarbons, 25 particularly a natural gas stream, according to which the liquefaction of the hydrocarbon-rich stream occurs in the heat exchange with a two-component refrigerant mixture stream; here one component is a constituent of the hydrocarbon-rich stream to be liquefied, while the other 30 component is a heavy hydrocarbon, preferably propane or propylene. Before cooling and refrigerating expansion of these components, a separation of the refrigerant mixture C:Nf.Par1l\DCOWANJEL1.O-JW0lJ into a higher boiling and a lower boiling refrigerant fraction takes place. Of disadvantage in the procedure described in 5 DE-A 102 09 799 is that the provision of two refrigerant components can lead to relatively large temperature differences in the heat exchangers. These temperature differences in turn require correspondingly high compressor capacities. 10 A similar method for liquefaction of a stream rich in hydrocarbons is known from US-A 6,347,531. In this method, the low pressure coolant is drawn cold through the circulation compressor, However, so-called cold-suctioning 15 compressors have the disadvantage that they are more difficult to operate than compressors which are not cold suctioning, especially during start-up and shutdown. A further disadvantage of the liquefaction process described in US-A 6,347,531 is that the refrigerant is partially 20 liquefied at an intermediate pressure, which results in greater equipment expense. One or more embodiments of the present invention may provide a generic method for liquefaction of a stream rich in 25 hydrocarbons, in particular a natural gas stream, which avoids the disadvantages of the known methods and in addition to that enables a lower specific energy requirement to be realised. 30 The present invention provides a method for liquefaction of a stream rich in hydrocarbons, in which: - the liquefaction of the hydrocarbon-rich stream takes -3 place in heat exchange with a refrigerant mixture comprising three or more components; - one of the components is a constituent of the hydrocarbon-rich stream to be liquefied; 5 - one of the components is propane, propylene or a C4 hydrocarbon; - one of the components is C2H4 or C2H6; the compression of the refrigerant mixture stream ensues by means of an at least two-stage compression; 10 - the refrigerant mixture is separated into a higher boiling fraction and a lower boiling refrigerant fraction, and the higher boiling fraction and the lower boiling refrigerant fraction are cooled and subjected to refrigerating expansion; 15 - the higher boiling fraction and lower boiling refrigerant fraction are supplied at the warm end of the heat exchange to said compression at different pressures after being subjected to refrigerating expansions; and - at least one substream of the lower boiling refrigerant 20 fraction is partially condensed and at least one liquid fraction is thus recovered, wherein at least a portion of said at least one liquid fraction recovered during the partial condensation(s) of said at least one substream of the lower boiling refrigerant 25 fraction is supercooled, expanded to the pressure of the higher boiling fraction and fed to the same compression stage as the higher boiling fraction. Surprisingly, it was found that the specific energy demand 30 of the liquefaction may be reduced by approximately 30% using certain embodiments of the inventive method. Furthermore, the temperature differences in the heat C:\NRPonblCCnVAMa DOC-23M2/20I -4 exchanger(s) may be considerably reduced. As a result, transient operation may be easier to control, In some embodiments of the inventive method for liquefaction S of a stream rich in hydrocarbons: - the stream rich in hydrocarbons is a stream of natural gas, the refrigerant mixture is a three-component refrigerant mixture, 10 - the refrigerant fractions are cooled separately, separately subjected to refrigerating expansion and separately heated against the hydrocarbon-rich stream to be liquefied, - a further component of the refrigerant mixture is 15 nitrogen, the compression of the refrigerant mixture stream takes place by means of an at least two-stage compression, and the higher boiling refrigerant fraction is added to the lower boiling refrigerant fraction at an 20 intermediate pressure stage, - at least one C 4 - to C 6 -hydrocarbon is used as a further component of the refrigerant mixture; the use of further refrigerant mixture components is particularly useful for larger liquefaction capacities of 10 tons 25 per hour or more, - another portion of said at least one liquid fraction recovered during the partial condensation(s) of said at least one substream of the lower boiling refrigerant fraction is supercooled, expanded to the pressure of 30 the lower boiling fraction and fed to the same compression stage as the lower boiling fraction, and/or the liquefaction of the hydrocarbon-rich stream takes - 4A place against the refrigerant mixture in one or more plate heat exchangers. The method according to the invention and further 5 embodiments thereof are explained in more detail below, by way of example only, based on the embodiment depicted in the figure. In accordance with the process depicted in the figure, a 10 dry, pre-treated stream rich in hydrocarbons, such as natural gas, is supplied via line X to the inventive liquefaction process, liquefied in the heat exchanger E and supercooled as required. The hydrocarbon-rich stream has a pressure between 10 and 60 bar, for example. The liquefied 15 and possibly supercooled hydrocarbon-rich stream is subsequently supplied via line Xr for its further use. Not shown in the figure is a possible separation to be provided for undesired components, such as heavier hydrocarbons. Reference is made in this regard to the corresponding 20 details in the aforementioned DE-A 102 09 799.
5 The cooling and liquefaction of the stream X, X' rich in hydrocarbons takes place in accordance with the invention in heat exchange with a refrigerant mixture stream comprising three or more components, in which one of the 5 components is a constituent of the hydrocarbon-rich stream - preferably methane - to be liquefied, one of the components is propane, propylene or a C 4 -hydrocarbon and one of the components is C 2
H
4 or C 2
H
6 . 10 The corresponding cooling circuit preferably has a two stage compressor unit consisting of the compressor stages Cl and C2. There is an air or water cooler, not shown in the figure, downstream from each compressor stage. Furthermore, the cooling circuit has a high pressure 15 separator D. The provision of only one high pressure separator D reduces the operating expense of the inventive process considerably compared to the known refrigerant mixture circuits. 20 The refrigerant mixture is separated into a lower boiling and a higher boiling fraction in the separator D. The lower boiling fraction is removed from the separator D via line 2, cooled in the heat exchanger E, condensed and supercooled and subsequently subjected to refrigerating 25 expansion in the expansion valve b on the cold end of the heat exchanger E. The expanded fraction is re-introduced via line 3 to the heat exchanger E, vaporised as well as superheated in it against the process streams to be cooled and subsequently fed via line 4 to the first 30 compressor stage C1. After compression cooling (not shown in the figure), the compressed lower boiling fraction is fed via line 8 to 6 the second compressor stage C2 - the addition of the higher boiling fraction is described in more detail below - where it is compressed to the desired final pressure of the circuit, which is between 20 and 60 bar, for example. 5 A heat exchanger, not shown in the figure, is also connected as a cooler downstream of the second compressor stage C2. The refrigerant mixture cooled and partially condensed in the heat exchanger is fed again via line 1 to the separator D. 10 A higher boiling liquid fraction is drawn off from the sump of the separator D via line 5, cooled in the heat exchanger E and subsequently subjected to refrigerating expansion to the desired intermediate pressure in the 15 expansion valve a. Afterward this fraction is introduced once again via line 6 to the heat exchanger, vaporised as well as superheated in it against the process streams to be cooled and then fed via line 7 to the compressor unit before its second compressor stage C2. 20 Corresponding to an advantageous embodiment of the inventive liquefaction process, at least one substream 9 of the lower boiling refrigerant fraction 2 can be drawn out via line 9 (depicted as a dashed line) from the heat 25 exchanger E after cooling and partial condensation and fed to a (so-called "cold") separator D' (depicted as a dashed rectangle). The gaseous fraction drawn off via line 10 (shown dashed) at the head of the separator D' is once again introduced to the heat exchanger E, 30 supercooled and expanded in valve b for the purpose of providing the peak cold required for the liquefaction process.
7 The liquid fraction drawn off via line 11 (shown dashed) from the sump of the separator D' is supercooled in the heat exchanger E, subjected to refrigerating expansion in valve c, fed via line 12 to the heat exchanger E and 5 added to the refrigerant fraction in line 3. Additional so-called "cold separators" can be provided after this separator D'. These lead to an improvement of the specific energy demand of the inventive liquefaction 10 process, but due to the additional equipment expense involved, they only make sense for larger liquefaction plants. The higher boiling fractions recovered in the separator 15 D' and any further "cold separators" are preferably supercooled, expanded to the pressure of the (first) higher boiling fraction and fed to the same compressor stage as the (first) higher boiling fraction. This embodiment of the inventive method is depicted in the 20 figure by the dotted line 13. Depending on the temperature profile in the heat exchanger E, addition to the low pressure refrigerant stream in the line segments 3 and 4 is expedient. 25 Corresponding to an advantageous embodiment of the inventive process, the liquefaction of the hydrocarbon rich takes place against the refrigerant mixture in plate heat exchangers. Based on the inventive method, the process control can be implemented in a single plate heat 30 exchanger for liquefaction plants with a liquefaction capacity of up to 10 to 15 tons per hour.
-8 The inventive method for liquefaction of a stream rich in hydrocarbons, in particular a natural gas stream, avoids all the disadvantages of the state of the art initially cited. 5 The reference in this specification to any prior publication (or information derived from it), or to any matter which is known, is not, and should not be taken as an acknowledgment or admission or any form of suggestion that that prior publication (or information derived from it) or known matter 10 forms part of the common general knowledge in the field of endeavour to which this specification relates. Throughout this specification and the claims which follow, unless the context requires otherwise, the word "comprise", 15 and variations such as "comprises" and "comprising", will be understood to imply the inclusion of a stated integer or step or group of integers or steps but not the exclusion of any other integer or step- or group of integers or steps.
Claims (10)
1. A method for liquefaction of a stream rich in hydrocarbons, in which: 5 - the liquefaction of the hydrocarbon-rich stream takes place in heat exchange with a refrigerant mixture comprising three or more components; - one of the components is a constituent of the hydrocarbon-rich stream to be liquefied; 10 - one of the components is propane, propylene or a C4 hydrocarbon; - one of the components is C
2 H 4 or C2H 6 ; - the compression of the refrigerant mixture stream ensues by means of an at least two-stage compression; 15 - the refrigerant mixture is separated into a higher boiling fraction and a lower boiling refrigerant fraction, and the higher boiling fraction and the lower boiling refrigerant fraction are cooled and subjected to refrigerating expansion; 20 - the higher boiling fraction and lower boiling refrigerant fraction are supplied at the warm end of the heat exchange to said compression at different pressures after being subjected to refrigerating expansions; and - at least one substream of the lower boiling refrigerant 25 fraction is partially condensed and at least one liquid fraction is thus recovered, wherein at least a portion of said at least one liquid fraction recovered during the partial condensation(s) of said at least one substream of the lower boiling refrigerant 30 fraction is supercooled, expanded to the pressure of the higher boiling fraction and fed to the same compression stage as the higher boiling fraction. - 10 2. A method according to claim 1, wherein the stream rich in hydrocarbons is a stream of natural gas. 5
3. A method according to claim 1 or 2, wherein the refrigerant mixture is a three-component refrigerant mixture.
4. A method according to claim 1, 2 or 3, wherein the 10 higher boiling fraction and the lower boiling refrigerant fraction are cooled separately, separately subjected to refrigerating expansion and separately heated against the hydrocarbon-rich stream to be liquefied. 15
5. A method according to any one of the preceding claims, wherein a further component of the refrigerant mixture is nitrogen.
6. A method according to any one of the preceding claims, 20 wherein at least one C 4 - to C 6 -hydrocarbon is used as a further component of the refrigerant mixture.
7. A method according to any one of the preceding claims, wherein another portion of said at least one liquid fraction 25 recovered during the partial condensation(s) of said at least one substream of the lower boiling refrigerant fraction is supercooled, expanded to the pressure of the lower boiling fraction and fed to the same compression stage as the lower boiling fraction. 30
8. A method according to any one of the preceding claims, wherein the liquefaction of the hydrocarbon-rich stream C:W.\N.dhCC\WANfM34,7/7TOC.DC2>/ZI'2I I - 11 takes place against the refrigerant mixture in one or more plate heat exchangers.
9. The method according to claim 8, wherein the S liquefaction takes place in a single plate heat exchanger.
10. The method according to claim 1 and substantially as hereinbefore described with reference to the accompanying drawing. 10
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102005010055A DE102005010055A1 (en) | 2005-03-04 | 2005-03-04 | Process for liquefying a hydrocarbon-rich stream |
| DE102005010055.4 | 2005-03-04 | ||
| PCT/EP2006/001804 WO2006094675A1 (en) | 2005-03-04 | 2006-02-28 | Method for liquefaction of a stream rich in hydrocarbons |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU2006222325A1 AU2006222325A1 (en) | 2006-09-14 |
| AU2006222325B2 true AU2006222325B2 (en) | 2011-03-24 |
Family
ID=36508129
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2006222325A Ceased AU2006222325B2 (en) | 2005-03-04 | 2006-02-28 | Method for liquefaction of a stream rich in hydrocarbons |
Country Status (10)
| Country | Link |
|---|---|
| US (1) | US20090205366A1 (en) |
| EP (1) | EP1864062A1 (en) |
| CN (1) | CN101189483A (en) |
| AU (1) | AU2006222325B2 (en) |
| BR (1) | BRPI0609292A2 (en) |
| CA (1) | CA2600027A1 (en) |
| DE (1) | DE102005010055A1 (en) |
| NO (1) | NO20075003L (en) |
| RU (1) | RU2007136598A (en) |
| WO (1) | WO2006094675A1 (en) |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102008019392A1 (en) * | 2008-04-17 | 2009-10-22 | Linde Aktiengesellschaft | Process for liquefying a hydrocarbon-rich fraction |
| US9441877B2 (en) | 2010-03-17 | 2016-09-13 | Chart Inc. | Integrated pre-cooled mixed refrigerant system and method |
| MY162011A (en) * | 2010-03-25 | 2017-05-31 | Univ Manchester | Refrigeration process |
| CN102336626B (en) * | 2010-07-28 | 2014-03-12 | 中国石油化工股份有限公司 | Utilization method of waste gas discharged from butadiene extracting apparatus |
| CN102304403B (en) * | 2011-08-08 | 2013-07-24 | 成都赛普瑞兴科技有限公司 | Method and device for liquefying natural gas by using propylene precooling mixed cryogen |
| KR101392750B1 (en) * | 2012-06-29 | 2014-05-09 | 한국에너지기술연구원 | Natural gas liquefaction system and method using the same |
| US11428463B2 (en) | 2013-03-15 | 2022-08-30 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
| US11408673B2 (en) | 2013-03-15 | 2022-08-09 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
| CN105473967B (en) * | 2013-03-15 | 2018-06-26 | 查特能源化工公司 | Mixed refrigerant systems and method |
| NO3001128T3 (en) * | 2013-05-20 | 2018-12-08 | ||
| KR101630518B1 (en) * | 2014-08-01 | 2016-06-14 | 한국가스공사 | Natural gas liquefaction process |
| KR101615443B1 (en) * | 2014-08-01 | 2016-04-25 | 한국가스공사 | Natural gas liquefaction process |
| AR105277A1 (en) | 2015-07-08 | 2017-09-20 | Chart Energy & Chemicals Inc | MIXED REFRIGERATION SYSTEM AND METHOD |
| CN107101456A (en) * | 2017-06-13 | 2017-08-29 | 江苏华滋海洋工程有限公司 | A kind of liquefied ethane boil-off gas reliquefaction installation peculiar to vessel |
| CN107436072B (en) * | 2017-08-14 | 2019-11-29 | 新地能源工程技术有限公司 | Natural gas liquefaction system and method with refrigerant supplementary device |
| FR3098574B1 (en) * | 2019-07-10 | 2021-06-25 | Air Liquide | Refrigeration and / or liquefaction device |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3747359A (en) * | 1969-08-01 | 1973-07-24 | Linde Ag | Gas liquefaction by a fractionally condensed refrigerant |
| GB1392972A (en) * | 1972-09-25 | 1975-05-07 | Petrocarbon Dev Ltd | Cooling fluids at low temperatures |
| US4094655A (en) * | 1973-08-29 | 1978-06-13 | Heinrich Krieger | Arrangement for cooling fluids |
| US4274849A (en) * | 1974-11-21 | 1981-06-23 | Campagnie Francaise d'Etudes et de Construction Technip | Method and plant for liquefying a gas with low boiling temperature |
| US4325231A (en) * | 1976-06-23 | 1982-04-20 | Heinrich Krieger | Cascade cooling arrangement |
| DE19612173C1 (en) * | 1996-03-27 | 1997-05-28 | Linde Ag | Procedure for liquefaction of hydrocarbon rich process flow, especially natural gas |
| US6347531B1 (en) * | 1999-10-12 | 2002-02-19 | Air Products And Chemicals, Inc. | Single mixed refrigerant gas liquefaction process |
| DE10209799A1 (en) * | 2002-03-06 | 2003-09-25 | Linde Ag | Process for liquefying a hydrocarbon-rich stream |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4404008A (en) * | 1982-02-18 | 1983-09-13 | Air Products And Chemicals, Inc. | Combined cascade and multicomponent refrigeration method with refrigerant intercooling |
| US4755200A (en) * | 1987-02-27 | 1988-07-05 | Air Products And Chemicals, Inc. | Feed gas drier precooling in mixed refrigerant natural gas liquefaction processes |
| MY118329A (en) * | 1995-04-18 | 2004-10-30 | Shell Int Research | Cooling a fluid stream |
| 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 |
-
2005
- 2005-03-04 DE DE102005010055A patent/DE102005010055A1/en not_active Withdrawn
-
2006
- 2006-02-28 WO PCT/EP2006/001804 patent/WO2006094675A1/en active Application Filing
- 2006-02-28 US US11/817,379 patent/US20090205366A1/en not_active Abandoned
- 2006-02-28 BR BRPI0609292-6A patent/BRPI0609292A2/en not_active IP Right Cessation
- 2006-02-28 CN CNA200680007021XA patent/CN101189483A/en active Pending
- 2006-02-28 RU RU2007136598/06A patent/RU2007136598A/en unknown
- 2006-02-28 CA CA002600027A patent/CA2600027A1/en not_active Abandoned
- 2006-02-28 AU AU2006222325A patent/AU2006222325B2/en not_active Ceased
- 2006-02-28 EP EP06707313A patent/EP1864062A1/en not_active Withdrawn
-
2007
- 2007-10-03 NO NO20075003A patent/NO20075003L/en not_active Application Discontinuation
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3747359A (en) * | 1969-08-01 | 1973-07-24 | Linde Ag | Gas liquefaction by a fractionally condensed refrigerant |
| GB1392972A (en) * | 1972-09-25 | 1975-05-07 | Petrocarbon Dev Ltd | Cooling fluids at low temperatures |
| US4094655A (en) * | 1973-08-29 | 1978-06-13 | Heinrich Krieger | Arrangement for cooling fluids |
| US4274849A (en) * | 1974-11-21 | 1981-06-23 | Campagnie Francaise d'Etudes et de Construction Technip | Method and plant for liquefying a gas with low boiling temperature |
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Also Published As
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|---|---|
| CN101189483A (en) | 2008-05-28 |
| US20090205366A1 (en) | 2009-08-20 |
| NO20075003L (en) | 2007-10-03 |
| BRPI0609292A2 (en) | 2010-03-09 |
| WO2006094675A1 (en) | 2006-09-14 |
| AU2006222325A1 (en) | 2006-09-14 |
| EP1864062A1 (en) | 2007-12-12 |
| CA2600027A1 (en) | 2006-09-14 |
| RU2007136598A (en) | 2009-04-10 |
| DE102005010055A1 (en) | 2006-09-07 |
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