AU2011201092A1 - Process for liquefying a hydrocarbon-rich fraction - Google Patents
Process for liquefying a hydrocarbon-rich fraction Download PDFInfo
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- AU2011201092A1 AU2011201092A1 AU2011201092A AU2011201092A AU2011201092A1 AU 2011201092 A1 AU2011201092 A1 AU 2011201092A1 AU 2011201092 A AU2011201092 A AU 2011201092A AU 2011201092 A AU2011201092 A AU 2011201092A AU 2011201092 A1 AU2011201092 A1 AU 2011201092A1
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- Australia
- Prior art keywords
- fraction
- boiling
- hydrocarbon
- rich
- 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.)
- Abandoned
Links
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 39
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 39
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 35
- 238000009835 boiling Methods 0.000 claims abstract description 91
- 239000007789 gas Substances 0.000 claims abstract description 46
- 239000007788 liquid Substances 0.000 claims abstract description 44
- 239000002826 coolant Substances 0.000 claims abstract description 33
- 239000000203 mixture Substances 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 25
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 14
- 230000008016 vaporization Effects 0.000 claims abstract description 13
- 239000003345 natural gas Substances 0.000 claims abstract description 7
- 238000009833 condensation Methods 0.000 claims abstract description 6
- 230000005494 condensation Effects 0.000 claims abstract description 6
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 210000003918 fraction a Anatomy 0.000 abstract description 2
- 239000007791 liquid phase Substances 0.000 description 10
- 230000002051 biphasic effect Effects 0.000 description 9
- 239000012071 phase Substances 0.000 description 6
- 238000009834 vaporization Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000012080 ambient air Substances 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
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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
- 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
-
- 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
- F25J1/02—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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
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)
Abstract
Abstract Process for liquefying a hydrocarbon-rich fraction A process is proposed for liquefying a hydrocarbon-rich fraction (A), especially natural gas, by 5 a) liquefying the hydrocarbon-rich fraction (A) against the coolant mixture of a cooling circuit, b) compressing the coolant mixture in at least two stages (C1, C2), c) partially condensing (El) the compressed coolant mixture (2) at least downstream of the penultimate compressor stage (Cl), 10 d) compressing (C2) the lower-boiling gas fraction (2') obtained to the final pressure, e) while cooling (E) the first higher-boiling liquid fraction (3) obtained, expanding it (a) to perform cooling and vaporizing it (E) against the hydrocarbon-rich fraction (A) to be cooled, 15 f) partially condensing (E2) the coolant mixture fraction (4) compressed to the final pressure and separating the first lower-boiling gas fraction (5) obtained, after partial condensation (E), into a second lower-boiling gas fraction (7) and a second higher-boiling liquid fraction (6), and g) liquefying and subcooling (E) the second lower-boiling gas fraction (7), sub 20 cooling (E) the second higher-boiling liquid fraction (6) and expanding the two fractions to different temperature levels to perform cooling (b, c), and partly heating and at least partly vaporizing them (E) against the hydrocarbon-rich fraction (A) to be cooled. According to the invention, the composition of the coolant mixture is selected such that 25 the final boiling point (dew point) of the second lower-boiling gas fraction (7) is at a lower temperature than the initial boiling point of the first higher-boiling liquid fraction (3). 30 (The figure relates thereto.) C14 CY) u ol 0) co P, ui
Description
- 1 AUSTRALIA PATENTS ACT 1990 COMPLETE SPECIFICATION FOR A STANDARD PATENT ORIGINAL Name of Applicant: Linde Aktiengesellschaft Actual Inventors: Heinz Bauer and 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 LIQUEFYING A HYDROCARBON-RICH FRACTION The following statement is a full description of this invention, including the best method of performing it known to me/us: File: 69496AUP00 la Description Process for liquefying a hydrocarbon-rich fraction The invention relates to a process for liquefying a hydrocarbon-rich fraction, especially natural gas, by 5 a) liquefying the hydrocarbon-rich fraction against the coolant mixture of a cooling circuit, b) compressing the coolant mixture in at least two stages, c) partially condensing the compressed coolant mixture at least downstream of the penultimate compressor stage, 10 d) compressing the lower-boiling gas fraction obtained to the final pressure, e) while cooling the first higher-boiling liquid fraction obtained, expanding it to perform cooling and vaporizing it against the hydrocarbon-rich fraction to be cooled, f) partially condensing the coolant mixture fraction compressed to the final 15 pressure and separating the first lower-boiling gas fraction obtained, after partial condensation, into a second lower-boiling gas fraction and a second higher boiling liquid fraction, and g) liquefying and subcooling the second lower-boiling gas fraction, subcooling the second higher-boiling liquid fraction and expanding the two fractions to different 20 temperature levels to perform cooling, and partly heating and at least partly vaporizing them against the hydrocarbon-rich fraction to be cooled. A process of this type for liquefying a hydrocarbon-rich fraction is known, for example, from German Patent Application 197 22 490, now Australian Patent No.745564. Such 25 processes for liquefying hydrocarbon-rich fractions are employed, for example, in natural gas liquefaction plants with a liquefaction performance between 10 000 and 3 000 000 t/a of LNG. With the citation of German Patent Application 197 22 490, the content thereof is incorporated in its entirety into the disclosure-content of the present application. 30 In the liquefaction process described with reference to Figure 2 of German Patent Application 197 22 490, the coolant mixture, in the course of the multistage compression thereof, is partially condensed after each compressor stage, typically 2 against ambient air and/or water. A first liquid phase obtained at an intermediate stage is used to precool the hydrocarbon-rich fraction to be liquefied. The first gas obtained at the highest pressure is likewise partially condensed and separated into a second gas phase and a second liquid phase. The second gas phase is liquefied, decompressed 5 and then partly vaporized in countercurrent to the hydrocarbon-rich fraction to be liquefied. The expanded second liquid phase, which is likewise present in biphasic form, is added to this partly vaporized coolant mixture stream. The aforementioned first liquid phase is, after the expansion thereof, added, likewise in biphasic form, to the aforementioned mixture stream of second gas phase and second liquid phase. 10 In practice, it is found that the mixing of two biphasic coolant streams has good technical controllability in what is called falling vaporization, as takes place, for example, on the outside of helically coiled heat exchangers. In the case of rising vaporization, as is typically implemented in plate heat exchangers, the biphasicity of 15 the two streams to be mixed, however, can lead to problems. Since such mixing of biphasic streams in a plate heat exchanger is not technically controllable at present, the two biphasic streams are mixed in a vessel outside the heat exchanger and separated into a gas phase and a liquid phase. Since the liquid phase has to be fed in from this vessel to the heat exchanger with a gradient, conduction of at least one 20 biphasic stream through an ascending line between the heat exchanger and the vessel is unavoidable. According to the load range, this can lead, however, to undesirable unstable flow forms and as a result to disrupted operation. Unless the context clearly requires otherwise, throughout the description and the 25 claims, the words "comprise", "comprising", and the like are to be construed in an inclusive sense as opposed to an exclusive or exhaustive sense; that is to say, in the sense of "including, but not limited to". It is an object of a preferred form of the present invention to specify a process of the 30 generic type for liquefying a hydrocarbon-rich fraction, which avoids the aforementioned disadvantages. It is an object of the present invention to overcome or ameliorate at least one of the disadvantages of the prior art, or to provide a useful alternative. 35 3 According to a first aspect, the present invention provides a process for liquefying a hydrocarbon-rich fraction by a) liquefying the hydrocarbon-rich fraction against the coolant mixture of a cooling 5 circuit, b) compressing the coolant mixture in at least two stages c) partially condensing the compressed coolant mixture at least downstream of the penultimate compressor stage d) compressing the lower-boiling gas fraction obtained to the final pressure, 10 e) while cooling the first higher-boiling liquid fraction obtained, expanding it to perform cooling and vaporizing it against the hydrocarbon-rich fraction to be cooled, f) partially condensing the coolant mixture fraction compressed to the final pressure and separating the first lower-boiling gas fraction obtained, after partial 15 condensation into a second lower-boiling gas fraction and a second higher boiling liquid fraction, and g) liquefying and subcooling the second lower-boiling gas fraction sub-cooling the second higher-boiling liquid fraction and expanding the two fractions to different temperature levels to perform cooling and partly heating and at least partly 20 vaporizing them against the hydrocarbon-rich fraction to be cooled, wherein the composition of the coolant mixture is selected such that the final boiling point (dew point) of the second lower-boiling gas fraction is at a lower temperature than the initial boiling point of the first higher-boiling liquid fraction. 25 According to a second aspect, the present invention provides a liquefied hydrocarbon rich fraction when produced by the process according to the invention. According to the invention, a process is proposed for liquefying a hydrocarbon-rich fraction, characterized in that the composition of the coolant mixture is selected such 30 that the final boiling point (dew point) of the second lower-boiling gas fraction is at a lower temperature than the initial boiling point of the first higher-boiling liquid fraction. According to the invention, the first higher-boiling liquid fraction is not now added to the second lower-boiling gas fraction until after the complete vaporization thereof. This 4 procedure dispenses with the provision of a biphasic riser line, described at the outset, between heat exchanger and vessel. Further advantageous configurations of the process according to the invention for 5 liquefying a hydrocarbon-rich fraction, which are the subjects of the independent claims, are characterized in that - the temperature difference between the final boiling point of the second lower boiling gas fraction and the initial boiling point of the first higher-boiling liquid 10 fraction is at least 5 K, preferably at least 10 K, - the second higher-boiling liquid fraction is vaporized separately from the first higher-boiling liquid fraction and the second lower-boiling gas fraction, 15 - the first higher-boiling liquid fraction and the second lower-boiling gas fraction are not combined until after they have been vaporized with the second higher boiling liquid fraction, - at least a substream of the cooled second lower-boiling gas fraction is added to 20 the expanded second higher-boiling liquid fraction, - expanded first higher-boiling liquid fraction and vaporized second lower-boiling gas fraction are mixed outside the heat exchanger(s) required for the heat exchange between the hydrocarbon-rich fraction to be liquefied and the cooling 25 circuit, preferably in a separator, the vaporized second lower-boiling gas fraction being supplied to the separator in monophasic form, - the liquid fraction obtained in the partial condensation of the coolant mixture fraction compressed to the final pressure subcools the first higher-boiling liquid 30 fraction. The process according to the invention for liquefying a hydrocarbon-rich fraction and further configurations thereof are explained in detail hereinafter with reference to the working example shown in the figure. 35 5 The figure shows a natural gas liquefaction process in which the natural gas to be liquefied is fed via line A to a heat exchanger E, liquefied against a coolant circuit and then drawn off via line B and sent to further use or storage thereof. The figure does not show any pretreatment steps to be provided for the natural gas to be liquefied, or any 5 removal of nitrogen and/or C2. hydrocarbons to be provided. The coolant mixture to be compressed in the coolant circuit is supplied via line 1 to a first separator D1 which is connected upstream of the compressor unit C1/C2 and serves to remove condensate. The gas phase obtained at the top of the separator D1 10 is fed via line 1' to the first compressor stage C1 and compressed to an intermediate pressure which is typically between 15 and 35 bar. The compressed coolant mixture is partially condensed in the heat exchanger El and fed via line 2 to a second separator D2. The first higher-boiling liquid fraction drawn off from the bottom of the separator D2 via line 3 is cooled in the heat exchanger E, decompressed to perform cooling in the 15 valve A and then added via line 3' to the coolant fraction in line 8, which will be discussed in more detail below. In an advantageous configuration of the invention, the expanded fraction 3' and the coolant fraction 8 can also be mixed outside the heat exchanger E. In this case, a separator should be provided, to which the two afore mentioned fractions are supplied, the coolant fraction 8 being supplied in monophasic 20 form. The gas phase drawn off from the separator D2 via line 2' is compressed in the second compressor stage C2 to the desired final pressure, which is typically between 25 and 70 bar. The coolant mixture compressed to the final pressure is partially condensed in 25 the heat exchanger E2 and fed via line 4 to a further separator D3. The liquid phase obtained in the separator D3 is recycled via line 4' upstream of the second separator D2. Appropriately, there is an exchange of heat between the liquid phases in lines 3 and 4' in the heat exchanger E3, which preferably serves to subcool 30 the liquid phase 3 drawn off from the bottom of the separator D2. Via line 5, a first lower-boiling gas fraction is drawn off at the top of the separator D3. This is partially condensed in the heat exchanger E and then supplied to a further separator D4 via line 5'. A separation is effected therein into a second higher-boiling 35 liquid fraction 6 and a second lower-boiling gas fraction 7. The second liquid fraction 6 6 is supplied to the heat exchanger E, subcooled therein and then expanded to perform cooling in the valve b. Via line sections 6' and 10, the expanded liquid fraction is fed again to the heat exchanger E or passed through it. 5 The second gas fraction 7 obtained at the top of the separator D4 is likewise first liquefied and then subcooled in the heat exchanger E. After it has been drawn off from the heater exchanger E, this fraction is divided into two substreams 8 and 9. Both substreams are expanded to perform cooling in the valves c or d. While one substream is conducted via line 8 through the heat exchanger E and is vaporized in heat 10 exchange against the hydrocarbon-rich stream to be liquefied, a further substream of the liquid fraction already mentioned can be added in the line 6'. This addition improves the controllability of temperature and cooling performance of stream 10, thus reducing the energy consumption, and/or serves to establish process conditions in the removal of nitrogen and/or C2. hydrocarbons from the hydrocarbon-rich fraction A to be 15 liquefied. As shown by the figure, the expanded second higher-boiling liquid fraction 6' is vaporized separately from the expanded first higher-boiling liquid fraction 3' and the expanded second lower-boiling gas fraction 8. This separate vaporization is effected in 20 separate flow channels of the heat exchanger E. The aforementioned fractions are therefore not mixed until the hot end of the heat exchanger E, when these fractions are completely vaporized. The separate vaporization leads to a slight increase in the energy consumption of the 25 liquefaction process of up to 3%; however, this can be accepted in view of the improved operability of the liquefaction process. The process according to the invention for liquefying a hydrocarbon-rich fraction now enables the unwanted rising biphasic flow, which was explained at the outset, outside 30 the heat exchanger to be avoided. The disrupted operation caused to date by this biphasic flow can consequently be ruled out.
Claims (12)
1. Process for liquefying a hydrocarbon-rich fraction by: a) liquefying the hydrocarbon-rich fraction against the coolant mixture of a cooling circuit, 5 b) compressing the coolant mixture in at least two stages, c) partially condensing the compressed coolant mixture at least downstream of the penultimate compressor stage, d) compressing the lower-boiling gas fraction obtained to the final pressure, e) while cooling the first higher-boiling liquid fraction obtained, expanding it to 10 perform cooling and vaporizing it against the hydrocarbon-rich fraction to be cooled, f) partially condensing the coolant mixture fraction compressed to the final pressure and separating the first lower-boiling gas fraction obtained, after partial condensation, into a second lower-boiling gas fraction and a second higher 15 boiling liquid fraction, and g) liquefying and subcooling the second lower-boiling gas fraction, sub-cooling the second higher-boiling liquid fraction and expanding the two fractions to different temperature levels to perform cooling, and partly heating and at least partly vaporizing them against the hydrocarbon-rich fraction to be cooled, 20 wherein the composition of the coolant mixture is selected such that the final boiling point (dew point) of the second lower-boiling gas fraction is at a lower temperature than the initial boiling point of the first higher-boiling liquid fraction.
2. Process according to Claim 1, wherein the temperature difference between the 25 final boiling point of the second lower-boiling gas fraction and the initial boiling point of the first higher-boiling liquid fraction is at least 5 K.
3. Process according to Claim 1, wherein the temperature difference between the final boiling point of the second lower-boiling gas fraction and the initial boiling 30 point of the first higher-boiling liquid fraction is at least 10 K.
4. Process according to any one of claims 1 to 3, wherein the second higher-boiling liquid fraction is vaporized separately from the first higher-boiling liquid fraction and the second lower-boiling gas fraction. 8
5. Process according to claim 4, wherein the first higher-boiling liquid fraction and the second lower-boiling gas fraction are not combined until after they have been vaporized with the second higher-boiling liquid fraction. 5
6. Process according to any one of the preceding claims wherein at least a substream of the cooled second lower-boiling gas fraction is added to the expanded second higher-boiling liquid fraction.
7. Process according to any one of the preceding claims, wherein expanded first 10 higher-boiling liquid fraction and vaporized second lower-boiling gas fraction are mixed outside the heat exchanger(s) required for the heat exchange between the hydrocarbon-rich fraction to be liquefied and the cooling circuit, the vaporized second lower-boiling gas fraction being supplied to the separator in monophasic form. 15
8. Process according to claim 7 wherein the expanded first higher-boiling liquid fraction and vaporized second lower-boiling gas fractions are mixed in a separator.
9. Process according to any one of the preceding claims, wherein the liquid fraction 20 obtained in the partial condensation of the coolant mixture fraction compressed to the final pressure subcools the first higher-boiling liquid fraction.
10. Process according to any one of the preceding claims wherein hydrocarbon-rich fraction is natural gas. 25
11. A liquefied hydrocarbon-rich fraction when produced by the process according to any one of the preceding claims.
12. A process for liquefying a hydrocarbon-rich fraction or a hydrocarbon-rich fraction 30 when produced by the process substantially as herein described with reference to any one of the embodiments of the invention illustrated in the accompanying drawings and/or examples.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102010011052A DE102010011052A1 (en) | 2010-03-11 | 2010-03-11 | Process for liquefying a hydrocarbon-rich fraction |
| DE102010011052.3 | 2010-03-11 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| AU2011201092A1 true AU2011201092A1 (en) | 2011-09-29 |
Family
ID=44507847
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2011201092A Abandoned AU2011201092A1 (en) | 2010-03-11 | 2011-03-10 | Process for liquefying a hydrocarbon-rich fraction |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20110219819A1 (en) |
| CN (1) | CN102200369A (en) |
| AU (1) | AU2011201092A1 (en) |
| BR (1) | BRPI1100950A2 (en) |
| DE (1) | DE102010011052A1 (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9441877B2 (en) | 2010-03-17 | 2016-09-13 | Chart Inc. | Integrated pre-cooled mixed refrigerant system and method |
| DE102011104725A1 (en) | 2011-06-08 | 2012-12-13 | Linde Aktiengesellschaft | Method for liquefying hydrocarbon rich fraction, particularly of natural gas, involves liquefying refrigerant mixture of refrigerant circuit against hydrocarbon-rich fraction |
| CN102748919A (en) * | 2012-04-26 | 2012-10-24 | 中国石油集团工程设计有限责任公司 | Single-cycle mixed-refrigerant four-stage throttling refrigeration system and method |
| DE102012008961A1 (en) * | 2012-05-03 | 2013-11-07 | Linde Aktiengesellschaft | Process for re-liquefying a methane-rich fraction |
| US11428463B2 (en) | 2013-03-15 | 2022-08-30 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
| ES2784619T3 (en) | 2013-03-15 | 2020-09-29 | 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 |
| DE102013016695A1 (en) * | 2013-10-08 | 2015-04-09 | Linde Aktiengesellschaft | Process for liquefying a hydrocarbon-rich fraction |
| CN104089463B (en) * | 2014-07-16 | 2017-11-17 | 北京安珂罗工程技术有限公司 | A kind of method and system of azeotrope gas-liquid separating throttling refrigeration |
| DE102014012316A1 (en) * | 2014-08-19 | 2016-02-25 | Linde Aktiengesellschaft | Process for cooling a hydrocarbon-rich fraction |
| AR105277A1 (en) | 2015-07-08 | 2017-09-20 | Chart Energy & Chemicals Inc | MIXED REFRIGERATION SYSTEM AND METHOD |
| EP3420289B1 (en) * | 2016-02-26 | 2022-12-21 | Lge Ip Management Company Limited | Method of cooling boil-off gas and apparatus therefor |
| GB201706265D0 (en) | 2017-04-20 | 2017-06-07 | Babcock Ip Man (Number One) Ltd | Method of cooling a boil-off gas and apparatus therefor |
| GB201912126D0 (en) * | 2019-08-23 | 2019-10-09 | Babcock Ip Man Number One Limited | Method of cooling boil-off gas and apparatus therefor |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4325231A (en) * | 1976-06-23 | 1982-04-20 | Heinrich Krieger | Cascade cooling arrangement |
| FR2703762B1 (en) * | 1993-04-09 | 1995-05-24 | Maurice Grenier | Method and installation for cooling a fluid, in particular for liquefying natural gas. |
| DE19716415C1 (en) * | 1997-04-18 | 1998-10-22 | Linde Ag | Process for liquefying a hydrocarbon-rich stream |
| DE19722490C1 (en) * | 1997-05-28 | 1998-07-02 | Linde Ag | Single flow liquefaction of hydrocarbon-rich stream especially natural gas with reduced energy consumption |
-
2010
- 2010-03-11 DE DE102010011052A patent/DE102010011052A1/en not_active Withdrawn
-
2011
- 2011-03-08 CN CN201110087116XA patent/CN102200369A/en active Pending
- 2011-03-09 US US13/043,944 patent/US20110219819A1/en not_active Abandoned
- 2011-03-10 AU AU2011201092A patent/AU2011201092A1/en not_active Abandoned
- 2011-03-11 BR BRPI1100950-0A patent/BRPI1100950A2/en not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| US20110219819A1 (en) | 2011-09-15 |
| BRPI1100950A2 (en) | 2012-08-07 |
| DE102010011052A1 (en) | 2011-09-15 |
| CN102200369A (en) | 2011-09-28 |
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| MK1 | Application lapsed section 142(2)(a) - no request for examination in relevant period |