CA2600027A1 - Method for liquefaction of a stream rich in hydrocarbons - Google Patents
Method for liquefaction of a stream rich in hydrocarbons Download PDFInfo
- Publication number
- CA2600027A1 CA2600027A1 CA002600027A CA2600027A CA2600027A1 CA 2600027 A1 CA2600027 A1 CA 2600027A1 CA 002600027 A CA002600027 A CA 002600027A CA 2600027 A CA2600027 A CA 2600027A CA 2600027 A1 CA2600027 A1 CA 2600027A1
- Authority
- CA
- Canada
- Prior art keywords
- fraction
- refrigerant
- hydrocarbon
- refrigerant mixture
- stream
- 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
- 238000000034 method Methods 0.000 title claims abstract description 35
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 34
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 34
- 239000003507 refrigerant Substances 0.000 claims abstract description 51
- 238000009835 boiling Methods 0.000 claims abstract description 36
- 239000000203 mixture Substances 0.000 claims abstract description 31
- 238000007906 compression Methods 0.000 claims abstract description 12
- 230000006835 compression Effects 0.000 claims abstract description 12
- 238000001816 cooling Methods 0.000 claims abstract description 7
- 238000000926 separation method Methods 0.000 claims abstract description 3
- 239000004215 Carbon black (E152) Substances 0.000 claims description 30
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 20
- 238000005057 refrigeration Methods 0.000 claims description 13
- 239000003345 natural gas Substances 0.000 claims description 10
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 8
- 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
- 230000005494 condensation Effects 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims 1
- 239000007788 liquid Substances 0.000 description 3
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000005265 energy consumption 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)
Abstract
The invention relates to a method for liquefaction of a stream rich in hydrocarbons, whereby the liquefaction of the stream (X, X' ) rich in hydrocarbons is carried out in heat exchange (E) with a three- or multi-component refrigerant mixture, the compression of the refrigerant mixture stream (4, 7) is carried out by means of an at least two-stage compression (Cl, C2), before the cooling (E) and the refrigerating expansion (a, b c) of the refrigerant mixture, a separation (D) of the refrigerant mixture into a higher boiling (5) and a lower boiling refrigerant fraction (2) is carried out and the higher boiling (5) and the lower boiling refrigerant fraction (2) are introduced (4, 7) to the compression (Cl, C2) after the refrigerating expansion (a, b, c) at the warm end of the heat exchanger (E).
Description
Description Process for Liquefying A Hydrocarbon-Rich Stream The invention relates to a process for liquefying a hydrocarbon-rich stream, specifically a natural gas stream.
Natural gas liquefaction plants are laid out either as what are known as LNG
baseload plants - plants for liquefying natural gas to provide natural gas as primary energy - or as what are known as peak shaving plants - plants for liquefying natural gas to meet peak demands.
Larger LNG plants are usually operated with refrigeration circuits which consist of hydrocarbon mixtures. These mixture circuits are more energy-efficient than expander circuits and allow relatively low specific energy consumption.
From DE-A 102 09 799 a process for liquefying a hydrocarbon-rich stream, specifically a natural gas stream, is known in accordance with which the liquefaction of the hydrocarbon-rich stream takes place in the heat exchange countercurrent to a two-component refrigerant mixture stream; the one component is a part of the hydrocarbon-rich stream to be liquefied, while the other component is a heavy hydrocarbon, preferably propane or propylene.
Before the cooling and the expansion to provide refrigeration of these components, the refrigerant mixture is separated into a higher boiling and a lower boiling refrigerant fraction.
A disadvantage of the procedure described in DE-A 102 09 799 is that providing two refrigerant components can result in relatively large temperature differences in the heat exchangers. These temperature differences in turn require correspondingly high compressor performance.
Natural gas liquefaction plants are laid out either as what are known as LNG
baseload plants - plants for liquefying natural gas to provide natural gas as primary energy - or as what are known as peak shaving plants - plants for liquefying natural gas to meet peak demands.
Larger LNG plants are usually operated with refrigeration circuits which consist of hydrocarbon mixtures. These mixture circuits are more energy-efficient than expander circuits and allow relatively low specific energy consumption.
From DE-A 102 09 799 a process for liquefying a hydrocarbon-rich stream, specifically a natural gas stream, is known in accordance with which the liquefaction of the hydrocarbon-rich stream takes place in the heat exchange countercurrent to a two-component refrigerant mixture stream; the one component is a part of the hydrocarbon-rich stream to be liquefied, while the other component is a heavy hydrocarbon, preferably propane or propylene.
Before the cooling and the expansion to provide refrigeration of these components, the refrigerant mixture is separated into a higher boiling and a lower boiling refrigerant fraction.
A disadvantage of the procedure described in DE-A 102 09 799 is that providing two refrigerant components can result in relatively large temperature differences in the heat exchangers. These temperature differences in turn require correspondingly high compressor performance.
A similar process for liquefying a hydrocarbon-rich stream is known from US
6, 347, 531. In this process, the low-pressure refrigerant is inducted cold through the circulating compressor. These cold-inducting compressors have the disadvantage that in operation, in particular during start-up and shut-down, they are more complicated to operate than compressors not inducting cold. Furthermore, in the liquefaction process described in US 6,347,531 it is disadvantageous that the refrigerant is partially liquefied at an intermediate pressure, which results in greater expense for equipment.
The object of the present invention is to specify a generic process for liquefying a hydrocarbon-rich stream, specifically of a natural gas stream, which avoids the disadvantages of the known processes and in addition allows a lower specific energy requirement to be realized.
To achieve this object, a generic process for liquefying a hydrocarbon-rich stream is proposed, wherein - the liquefaction of the hydrocarbon-rich stream takes place in the heat exchange countercurrent to a three- or multi-component refrigerant mixture, - one of the components is a part of the hydrocarbon-rich stream to be liquefied, - 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 takes place by means of an at least two-stage compression, - before the cooling and the expansion of the refrigerant mixture to provide refrigeration, the refrigerant mixture is separated into a higher boiling and a lower boiling refrigerant fraction and - the higher boiling and the lower boiling refrigerant fractions, after their expansion to provide refrigeration are taken at different pressures to compression.
Surprisingly, it has been shown that the specific expenditure of energy for liquefaction by means of the process in accordance with the invention can be reduced by approximately 30%. Furthermore, the temperature differences within the heat exchanger or heat exchangers can be reduced significantly.
The result is that transient operation is easier to control.
Additional advantageous embodiments of the process in accordance with the invention for liquefying a hydrocarbon-rich stream are:
- the refrigerant mixture is a three-component refrigerant mixture - the refrigerant fractions are cooled separately, expanded separately to provide refrigeration and heated separately countercurrent to the hydrocarbon-rich stream to be liquefied - a further component of the refrigerant mixture is nitrogen - compression of the refrigerant mixture stream takes place by means of an at least two-stage compression and the higher boiling refrigerant fraction is admixed to the lower boiling refrigerant fraction at an intermediate pressure level - at least one C4 to C6 hydrocarbon is used as further component(s) of the refrigerant mixture; the use of additional refrigerant components makes sense in particular at greater liquefaction outputs above 10 t/h.
- at least one partial stream of the lower boiling refrigerant fractions is partially condensed and the liquid fraction obtained thereby is supercooled and expanded.
6, 347, 531. In this process, the low-pressure refrigerant is inducted cold through the circulating compressor. These cold-inducting compressors have the disadvantage that in operation, in particular during start-up and shut-down, they are more complicated to operate than compressors not inducting cold. Furthermore, in the liquefaction process described in US 6,347,531 it is disadvantageous that the refrigerant is partially liquefied at an intermediate pressure, which results in greater expense for equipment.
The object of the present invention is to specify a generic process for liquefying a hydrocarbon-rich stream, specifically of a natural gas stream, which avoids the disadvantages of the known processes and in addition allows a lower specific energy requirement to be realized.
To achieve this object, a generic process for liquefying a hydrocarbon-rich stream is proposed, wherein - the liquefaction of the hydrocarbon-rich stream takes place in the heat exchange countercurrent to a three- or multi-component refrigerant mixture, - one of the components is a part of the hydrocarbon-rich stream to be liquefied, - 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 takes place by means of an at least two-stage compression, - before the cooling and the expansion of the refrigerant mixture to provide refrigeration, the refrigerant mixture is separated into a higher boiling and a lower boiling refrigerant fraction and - the higher boiling and the lower boiling refrigerant fractions, after their expansion to provide refrigeration are taken at different pressures to compression.
Surprisingly, it has been shown that the specific expenditure of energy for liquefaction by means of the process in accordance with the invention can be reduced by approximately 30%. Furthermore, the temperature differences within the heat exchanger or heat exchangers can be reduced significantly.
The result is that transient operation is easier to control.
Additional advantageous embodiments of the process in accordance with the invention for liquefying a hydrocarbon-rich stream are:
- the refrigerant mixture is a three-component refrigerant mixture - the refrigerant fractions are cooled separately, expanded separately to provide refrigeration and heated separately countercurrent to the hydrocarbon-rich stream to be liquefied - a further component of the refrigerant mixture is nitrogen - compression of the refrigerant mixture stream takes place by means of an at least two-stage compression and the higher boiling refrigerant fraction is admixed to the lower boiling refrigerant fraction at an intermediate pressure level - at least one C4 to C6 hydrocarbon is used as further component(s) of the refrigerant mixture; the use of additional refrigerant components makes sense in particular at greater liquefaction outputs above 10 t/h.
- at least one partial stream of the lower boiling refrigerant fractions is partially condensed and the liquid fraction obtained thereby is supercooled and expanded.
The process in accordance with the invention and additional embodiments of said invention which represent subjects of the dependent claims, are to be explained in what follows using the embodiment shown in the drawing.
In accordance with the procedure shown in the drawing, a dry, pre-treated hydrocarbon-rich stream, for example natural gas, is taken to the liquefaction process in accordance with the invention through line X and liquefied in heat exchanger E and supercooled if required. The hydrocarbon-rich stream is, as an example, at a pressure of between 10 and 60 bar. The liquefied and, if necessary supercooled, hydrocarbon-rich stream is then taken through line X' for further use. Not shown in the drawing is a separation, which may have to be provided, of undesirable components, for example higher hydrocarbons.
For this, reference is made to the appropriate explanations in the aforementioned DE-A 102 09 799.
The cooling and liquefaction of the hydrocarbon-rich stream X, X' takes place in accordance with the invention in the heat exchange countercurrent to a three or more component refrigerant mixture stream where one of the components is part of the hydrocarbon-rich stream to be liquefied -preferably methane - one of the components is propane, propylene or a C4 hydrocarbon and one of the components is C2H4 or C2H6.
The corresponding refrigeration circuit preferably has a two-stage compressor unit, consisting of the compressor stages Cl and C2. An air or water cooler -not shown in the drawing - is located in series with each compressor stage.
The refrigeration circuit further has a high-pressure extractor D. Providing only one high-pressure separator D reduces the operating cost of the process in accordance with the invention substantially - compared with the known refrigerant mixture circuits.
In the separator D, the refrigerant mixture is separated into a lower boiling and a higher boiling fraction. The lower boiling fraction is removed from the separator D through line 2, cooled in the heat exchanger E, condensed and supercooled and then expanded at the cold end of the heat exchanger E in expansion valve b, providing refrigeration. The expanded fraction is again taken to the heat exchanger E through line 3, evaporated and superheated therein countercurrent to process streams to be cooled and then taken to the first compressor stage Cl through line 4.
Following compression and cooling not shown in the drawing, the compressed lower boiling fraction is taken to the second compressor stage C2 through line 8 - the admixture of the higher boiling fraction will be discussed in more detail in what follows - and compressed to the desired circulation pressure which is, for example, between 20 and 60 bar. A heat exchanger as cooler not shown in the drawing is also located in series with the second compressor stage C2. The refrigerant mixture cooled and partially condensed in said cooler is taken back to the separator D through line 1.
A higher boiling liquid fraction is drawn off from the bottom of the separator D through line 5, cooled in the heat exchanger E and then expanded in expansion valve a to the desired intermediate pressure, providing refrigeration. Then this fraction is taken back to the heat exchanger E
through line 6, evaporated and superheated therein countercurrent to process streams to be cooled and then taken through line 7 to the compressor unit ahead of its second compressor stage C2.
In accordance with an advantageous embodiment of the liquefaction process in accordance with the invention, at least one partial stream 9 of the lower boiling refrigerant fraction 2 can be drawn off from the heat exchanger following cooling and partial condensation through the broken line 9, and taken to ("cold") separator D' indicated by broken lines. The gaseous fraction drawn off at the head of the separator D' through line 10 indicated by broken lines, is again returned to the heat exchanger E, supercooled and expanded for the purpose of providing the peak cold in valve b required for the liquefaction process.
The liquid fraction drawn off from the bottom of the separator D' through the broken line 11 is supercooled in the heat exchanger E, expanded in valve c providing refrigeration, taken to the heat exchanger E through line 12 and admixed to the refrigerant fraction in line 3.
Additional "cold separators" can be provided in addition to this separator D'.
They result in an improvement of the specific energy requirement of the liquefaction process in accordance with the invention, but they make sense only in larger liquefaction plants because of the additional expense required for equipment.
The higher boiling fractions recovered in the separator D' and any additional "cold separators" are preferably supercooled, expanded to the pressure of the (first) higher boiling fraction and taken to the compressor stage to which the (first) higher boiling fraction is also taken. This embodiment of the process in accordance with the invention is indicated in the drawing by the dotted line 13. Depending on the temperature profile in the heat exchanger E, admixture to the low-pressure refrigerant stream in line sections 3 and 4 also makes sense.
In accordance with an advantageous embodiment of the inventive process, the liquefaction of the hydrocarbon-rich stream takes place countercurrent to the refrigerant mixture in plate heat exchangers. Because of the process management in accordance with the invention, process management can be realized in a single plate heat exchanger in liquefaction plants having a liquefaction capacity of up to 10 to 15 t/h.
The process in accordance with the invention to liquefy a hydrocarbon-rich stream, specifically a natural gas stream, avoids all the disadvantages of the prior art cited at the beginning.
In accordance with the procedure shown in the drawing, a dry, pre-treated hydrocarbon-rich stream, for example natural gas, is taken to the liquefaction process in accordance with the invention through line X and liquefied in heat exchanger E and supercooled if required. The hydrocarbon-rich stream is, as an example, at a pressure of between 10 and 60 bar. The liquefied and, if necessary supercooled, hydrocarbon-rich stream is then taken through line X' for further use. Not shown in the drawing is a separation, which may have to be provided, of undesirable components, for example higher hydrocarbons.
For this, reference is made to the appropriate explanations in the aforementioned DE-A 102 09 799.
The cooling and liquefaction of the hydrocarbon-rich stream X, X' takes place in accordance with the invention in the heat exchange countercurrent to a three or more component refrigerant mixture stream where one of the components is part of the hydrocarbon-rich stream to be liquefied -preferably methane - one of the components is propane, propylene or a C4 hydrocarbon and one of the components is C2H4 or C2H6.
The corresponding refrigeration circuit preferably has a two-stage compressor unit, consisting of the compressor stages Cl and C2. An air or water cooler -not shown in the drawing - is located in series with each compressor stage.
The refrigeration circuit further has a high-pressure extractor D. Providing only one high-pressure separator D reduces the operating cost of the process in accordance with the invention substantially - compared with the known refrigerant mixture circuits.
In the separator D, the refrigerant mixture is separated into a lower boiling and a higher boiling fraction. The lower boiling fraction is removed from the separator D through line 2, cooled in the heat exchanger E, condensed and supercooled and then expanded at the cold end of the heat exchanger E in expansion valve b, providing refrigeration. The expanded fraction is again taken to the heat exchanger E through line 3, evaporated and superheated therein countercurrent to process streams to be cooled and then taken to the first compressor stage Cl through line 4.
Following compression and cooling not shown in the drawing, the compressed lower boiling fraction is taken to the second compressor stage C2 through line 8 - the admixture of the higher boiling fraction will be discussed in more detail in what follows - and compressed to the desired circulation pressure which is, for example, between 20 and 60 bar. A heat exchanger as cooler not shown in the drawing is also located in series with the second compressor stage C2. The refrigerant mixture cooled and partially condensed in said cooler is taken back to the separator D through line 1.
A higher boiling liquid fraction is drawn off from the bottom of the separator D through line 5, cooled in the heat exchanger E and then expanded in expansion valve a to the desired intermediate pressure, providing refrigeration. Then this fraction is taken back to the heat exchanger E
through line 6, evaporated and superheated therein countercurrent to process streams to be cooled and then taken through line 7 to the compressor unit ahead of its second compressor stage C2.
In accordance with an advantageous embodiment of the liquefaction process in accordance with the invention, at least one partial stream 9 of the lower boiling refrigerant fraction 2 can be drawn off from the heat exchanger following cooling and partial condensation through the broken line 9, and taken to ("cold") separator D' indicated by broken lines. The gaseous fraction drawn off at the head of the separator D' through line 10 indicated by broken lines, is again returned to the heat exchanger E, supercooled and expanded for the purpose of providing the peak cold in valve b required for the liquefaction process.
The liquid fraction drawn off from the bottom of the separator D' through the broken line 11 is supercooled in the heat exchanger E, expanded in valve c providing refrigeration, taken to the heat exchanger E through line 12 and admixed to the refrigerant fraction in line 3.
Additional "cold separators" can be provided in addition to this separator D'.
They result in an improvement of the specific energy requirement of the liquefaction process in accordance with the invention, but they make sense only in larger liquefaction plants because of the additional expense required for equipment.
The higher boiling fractions recovered in the separator D' and any additional "cold separators" are preferably supercooled, expanded to the pressure of the (first) higher boiling fraction and taken to the compressor stage to which the (first) higher boiling fraction is also taken. This embodiment of the process in accordance with the invention is indicated in the drawing by the dotted line 13. Depending on the temperature profile in the heat exchanger E, admixture to the low-pressure refrigerant stream in line sections 3 and 4 also makes sense.
In accordance with an advantageous embodiment of the inventive process, the liquefaction of the hydrocarbon-rich stream takes place countercurrent to the refrigerant mixture in plate heat exchangers. Because of the process management in accordance with the invention, process management can be realized in a single plate heat exchanger in liquefaction plants having a liquefaction capacity of up to 10 to 15 t/h.
The process in accordance with the invention to liquefy a hydrocarbon-rich stream, specifically a natural gas stream, avoids all the disadvantages of the prior art cited at the beginning.
Claims (7)
1. Process for liquefying a hydrocarbon-rich stream, specifically a natural gas stream, wherein - the liquefaction of the hydrocarbon-rich stream (X, X') takes place in the heat exchange (E) countercurrent to a three or more component refrigerant mixture, - one of the components is a part of the hydrocarbon-rich stream to be liquefied, - one of the components is propane, propylene or a C4 hydrocarbon, - one of the components is C2H4 or C2H6, - compression of the refrigerant mixture stream (4, 7) is carried out by means of an at least two-stage compression (C1, C2), - before the cooling (E) and expansion (a, b, c) of the refrigerant mixture to provide refrigeration, separation (D) of the refrigerant mixture into a higher boiling (5) and a lower boiling refrigerant fraction (2) takes place, - the higher boiling (5) and the lower boiling refrigerant fraction (2) are taken (4, 7) at different pressures for compression (C1, C2) following their expansion (a, b, c) at the hot end of the heat exchange (E) to provide refrigeration and - at least one partial stream (9) of the lower boiling refrigerant fraction (2) is partially condensed (D') and the fluid fraction recovered (11) is supercooled (E) and expanded (c), characterized in that the additional higher boiling fraction (11) recovered in the or the partial condensation (D') of one or several partial streams of the lower boiling refrigerant fraction (2) is supercooled, expanded to the pressure of the higher boiling fraction (6, 7) and taken (13) to the compressor stage (C2) to which the higher boiling fraction (6, 7) is also taken.
2. Process from claim 1, wherein the refrigerant mixture is a three-component refrigerant mixture.
3. Process from claim 1, wherein the refrigerant fraction (2, 5) is cooled separately (e), expanded separately to provide refrigeration (a, b, c) and heated (E) separately countercurrent to the hydrocarbon-rich stream (X, X') to be liquefied.
4. Process from one of the preceding claims 1 to 3, wherein a further component of the refrigerant mixture is nitrogen.
5. Process from one of the preceding claims 1 to 4, wherein at least one C4 to C6 hydrocarbon is, or are, used as (an) additional component(s) of the refrigerant mixture.
6. Process from one of the preceding claims 1 to 5, wherein the additional higher boiling fraction (11) recovered in the or the partial condensation (D') of one or several partial streams of the lower boiling refrigerant fraction (2) is supercooled, expanded to the pressure of the lower boiling fraction (3, 4) and taken to the compressor stage (C1) to which the lower boiling fraction (3, 4) is also taken.
7. Process from one of the preceding claims 1 to 6, wherein the liquefaction of the hydrocarbon-rich stream (X, X') takes place countercurrent to the refrigerant mixture in plate heat exchangers, preferably in a single plate heat exchanger (E).
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102005010055.4 | 2005-03-04 | ||
| DE102005010055A DE102005010055A1 (en) | 2005-03-04 | 2005-03-04 | Process for liquefying a hydrocarbon-rich stream |
| PCT/EP2006/001804 WO2006094675A1 (en) | 2005-03-04 | 2006-02-28 | Method for liquefaction of a stream rich in hydrocarbons |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2600027A1 true CA2600027A1 (en) | 2006-09-14 |
Family
ID=36508129
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002600027A Abandoned CA2600027A1 (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 |
| AU2011231314B2 (en) * | 2010-03-25 | 2016-02-04 | The University Of 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 |
| WO2014146138A1 (en) * | 2013-03-15 | 2014-09-18 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
| 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 |
| WO2014189261A1 (en) * | 2013-05-20 | 2014-11-27 | 한국가스공사 | Natural gas liquefaction process |
| 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 |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1939114B2 (en) * | 1969-08-01 | 1979-01-25 | Linde Ag, 6200 Wiesbaden | Liquefaction process for gases and gas mixtures, in particular for natural gas |
| 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 |
| FR2292203A1 (en) * | 1974-11-21 | 1976-06-18 | Technip Cie | METHOD AND INSTALLATION FOR LIQUEFACTION OF A LOW BOILING POINT GAS |
| US4325231A (en) * | 1976-06-23 | 1982-04-20 | Heinrich Krieger | Cascade cooling arrangement |
| 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 |
| 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 |
| 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 |
| DE10209799A1 (en) * | 2002-03-06 | 2003-09-25 | Linde Ag | Process for liquefying a hydrocarbon-rich stream |
-
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 AU AU2006222325A patent/AU2006222325B2/en not_active Ceased
- 2006-02-28 EP EP06707313A patent/EP1864062A1/en not_active Withdrawn
- 2006-02-28 US US11/817,379 patent/US20090205366A1/en not_active Abandoned
- 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 BR BRPI0609292-6A patent/BRPI0609292A2/en not_active IP Right Cessation
-
2007
- 2007-10-03 NO NO20075003A patent/NO20075003L/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| EP1864062A1 (en) | 2007-12-12 |
| WO2006094675A1 (en) | 2006-09-14 |
| NO20075003L (en) | 2007-10-03 |
| CN101189483A (en) | 2008-05-28 |
| US20090205366A1 (en) | 2009-08-20 |
| RU2007136598A (en) | 2009-04-10 |
| AU2006222325A1 (en) | 2006-09-14 |
| AU2006222325B2 (en) | 2011-03-24 |
| DE102005010055A1 (en) | 2006-09-07 |
| BRPI0609292A2 (en) | 2010-03-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2600027A1 (en) | Method for liquefaction of a stream rich in hydrocarbons | |
| RU2253809C2 (en) | Mode of liquefaction of natural gas by way of cooling at the expense of expansion | |
| US6253574B1 (en) | Method for liquefying a stream rich in hydrocarbons | |
| JP4741468B2 (en) | Integrated multi-loop cooling method for gas liquefaction | |
| RU2331826C2 (en) | Combined cycle of gas liquefaction, utilising multitude of expansion engine | |
| US6347531B1 (en) | Single mixed refrigerant gas liquefaction process | |
| KR100962627B1 (en) | Integrated multiple-loop refrigeration process for gas liquefaction | |
| EA002617B1 (en) | Plant for liquefying natural gas | |
| CN103591767A (en) | Liquefaction method and system | |
| JP3965444B2 (en) | Methods and equipment for natural gas liquefaction | |
| CN107869881B (en) | Mixed refrigerant cooling process and system | |
| NO20191220A1 (en) | Arctic Cascade method for natural gas liquefaction in a high-pressure cycle with pre-cooling by ethane and sub-cooling by nitrogen, and a plant for its implementation | |
| CA3040865C (en) | Method and system for cooling a hydrocarbon stream using a gas phase refrigerant | |
| NO311461B1 (en) | Process and apparatus for cooling fluids, especially for liquefaction of natural gas | |
| KR20110122101A (en) | Method and system for producing liquified natural gas | |
| AU2011321145B2 (en) | Natural gas liquefaction process | |
| RU2482405C2 (en) | Method for start of refrigerating circuit containing mixture of hydrocarbons | |
| US5579655A (en) | Process and apparatus for the liquefaction of hydrogen | |
| RU2725914C1 (en) | Method of liquefying a hydrocarbon-rich fraction | |
| CA2898745A1 (en) | Process for cooling a hydrocarbon-rich fraction | |
| EP0990108B1 (en) | Two staged refrigeration cycle using a multiconstituant refrigerant | |
| RU2556731C2 (en) | Method to liquefy natural gas by cooling mixtures, containing at least one non-saturated hydrocarbon | |
| AU2017202953A1 (en) | Natural gas liquefaction process | |
| KR101123977B1 (en) | Natural gas liquefaction process and system using the same | |
| US11604025B2 (en) | Standalone high-pressure heavies removal unit for LNG processing |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Discontinued |