Method for liquefying a stream rich in hydrocarbons

Abstract

The invention relates to a method for liquefying a stream rich in hydrocarbons, especially a stream of natural gas, by the indirect exchange of heat with the refrigerants in a closed-circuit cascade of mixed refrigerants. According to the invention, said closed-circuit cascade of mixed refrigerants consists of at least 3 circuits of mixed refrigerants, with each circuit comprising different refrigerants. The first of the three mixed refrigerant circuits is used for pre-cooling (E1), the second for liquefying E2), and the third for super-cooling (E3) the hydrocarbon-rich stream (1) to be liquefied. The method provided for in the invention reduces specific energy consumption and investment costs since the three circuits of mixed refrigerants are or can be optimally adjusted to the enthalpy temperature curves of the hydrocarbon-rich stream to be liquefied and the refrigerant mixtures.

Description

The invention relates to a, process for liquefying a hydrocarbon-rich stream, in particular a natural gas stream, by indirect heat exchange with the refrigerants of a mixed-refrigerant cascade cycle.

Pretreatment steps for the hydrocarbon-rich stream which may be necessary prior to the liquefaction, such as removal of acid gas and/or mercury, removal of aromatic components, etc. which are not subject-matter of the present invention, are not considered in detail below.

Currently, most base load LNG plants are designed as what are known as dual-flow refrigeration processes. In this case, the refrigeration energy required for liquefying the hydrocarbon-rich stream or the natural gas is provided by two separate mixed-refrigerant cycles which are connected to form one mixed-refrigerant cascade cycle. A liquefaction process of this type is disclosed, for example, by GB-B 895 094.

In addition, liquefaction processes are known, in which the refrigeration energy required for the liquefaction is provided by a refrigerant cascade cycle, but not, however, a mixed-refrigerant cascade cycle; see, for example, LINDE-Berichte aus Technik und Wissenschaft, Issue 75/1997, pages 3-8. The refrigerant cascade cycle described therein consists of a propane or propylene refrigeration cycle, an ethane or ethylene refrigeration cycle and a methane refrigeration cycle. Although this refrigerant cascade cycle can be considered as energetically optimized, it is comparatively complicated because of the 9 compressor stages.

In addition, liquefaction processes are known, as described, for example, in DE-B 19 60 301, in which the refrigeration energy required for the liquefaction is provided by a cascade consisting of a mixed-refrigerant cycle and a propane precooling cycle.

The object of the present invention is to specify a process for liquefying a hydrocarbon-rich stream, in particular a natural gas stream, which has a reduced specific energy consumption in comparison with dual-flow refrigeration processes of this type and thus makes it possible to implement a smaller plant size and, associated therewith, makes possible lower capital costs.

This object is achieved according to the invention by means of the fact that the mixed-refrigerant cascade cycle consists of at least 3 mixed-refrigerant cycles having different refrigerant compositions.

In the process according to the invention—known as triple-flow mixed-refrigerant cycle—the mixed-refrigerant cascade cycle consists of at least three separate mixed-refrigerant cycles. These have different refrigerant compositions, since they must produce refrigeration at different temperatures.

The first of the three mixed-refrigerant cycles—known as the Precooling Refrigerant Cycle (PRC)—serves for the cooling and partial or complete condensation of the mixed refrigerants required for the liquefaction and subcooling and for the precooling of the hydrocarbon-rich stream. The second mixed-refrigerant cycle—known as the Liquefaction Refrigerant Cycle (LRC)—serves for the partial or complete condensation of the mixed refrigerant required for the subcooling and the condensation of the hydro-carbon-rich stream. The third mixed-refrigerant cycle—known as the Subcooling Refrigerant Cycle (SRC)—serves for the necessary subcooling of the liquefied hydrocarbon-rich stream.

According to a further advantageous development of the process according to the invention, the refrigerant used for the first of the three mixed-refrigerant cycles is a mixture of ethylene or ethane, propane and butane. This PRC mixed-refrigerant cycle serves for providing refrigerant in a temperature range from ambient temperature to between approximately −35 and approximately −55° C. According to a further development of the process according to the invention, the refrigerant used for the second of the three mixed-refrigerant cycles is a mixture of methane, ethylene or ethane and propane. For the third of the three mixed-refrigerant cycles, the refrigerant preferably used is a mixture of nitrogen, methane and ethylene or ethane. While the second or LRC mixed-refrigerant cycle provides refrigeration energy in a temperature interval from approximately −40 to approximately −100° C., the third or SRC mixed-refrigerant cycle serves for providing refrigeration to between approximately −85 and approximately −160° C.

The process procedure according to the invention leads to a reduction of the specific energy consumption and of the capital costs, since the three mixed-refrigerant cycles are optimally adapted, or can be adapted, to the enthalpy-temperature graphs of the hydrocarbon-rich stream to be liquefied and of the mixed refrigerants. Owing to this process procedure which is more efficient in comparison with a dual-flow refrigeration process, either the liquefaction plant required may be decreased in size and thus the costs of the plant may be decreased, or the capacity of the hydrocarbon-rich stream to be liquefied can be increased with the plant size remaining the same.

BRIEF DESCRIPTION OF DRAWINGS

The process according to the invention and other developments of the same may now be described in more detail with reference to FIGS. 1 to 5 which are flowsheets of embodiments of the invention.

In the process according to the invention, the refrigerant required for liquefying the hydrocarbon-rich stream is provided by at least three mixed-refrigerant cycles. For the sake of clarity, in FIGS. 1 to 5 , a “P”, “L” or “S” for PRC, LRC or SRC mixed-refrigerant cycle is placed in front of each of the reference numbers for the individual mixed-refrigerant cycles.

According to the process shown in FIG. 1 , an optionally pretreated natural gas stream which has a temperature between 10 and 40° C. and a pressure between 30 and 70 bar is fed via line 1 to a first heat exchanger E 1 . In this heat exchanger E 1 , the natural gas stream is precooled to a temperature between −35 and −55° C. against a mixed refrigerant, expanded in an expansion valve P 13 , of the first or PRC mixed-refrigerant cycle in line P 14 .

The mixed refrigerant of the third or SRC mixed-refrigerant cycle is fed to the heat exchanger E 1 via line S 5 at a temperature between 10 and 40° C. and a pressure between 30 and 60 bar and is cooled and partially condensed in the heat exchanger E 1 against the abovementioned mixed refrigerant in line P 14 , the mixed refrigerant vaporizing in line P 14 at a pressure between 2 and 6 bar. The mixed refrigerant of the SRC mixed-refrigerant cycle leaves the heat exchanger E 1 via line S 6 at a temperature between −35 and −55° C.

The mixed refrigerant of the second or LRC mixed-refrigerant cycle is fed to the heat exchanger E 1 via line L 5 at a temperature between 10 and 40° C. and a pressure between 15 and 25 bar and is condensed in the heat exchanger E 1 against the mixed refrigerant of the PRC mixed-refrigerant cycle in line P 14 . The mixed refrigerant of the LRC mixed-refrigerant cycle is taken off from the heat exchanger E 1 at a temperature between −35 and −55° C.

The vaporized and superheated mixed refrigerant of the PRC mixed-refrigerant cycle in line P 14 essentially comprises, according to an advantageous development of the process according to the invention, 0 to 40 mol % ethylene or ethane, 30 to 40 mol % propane and 20 to 30 mol % butane. This mixed refrigerant is fed to the separator P 1 at a pressure of 2 to 6 bar. The gaseous mixed refrigerant taken off at the top of the separator P 1 via line P 2 is compressed in the compressor P 3 to a pressure between 6 and 10 bar. The compressed mixed refrigerant is subsequently cooled in the cooler P 4 to a temperature between 10 and 40° C., preferably against sea water, against air, or against a suitable coolant medium.

Subsequently thereto, the mixed refrigerant is fed via line P 5 to a further separator P 6 . The gaseous fraction of the mixed refrigerant produced at the top of the separator P 6 is fed to the second compressor stage P 8 and compressed in this to a pressure between 10 and 20 bar. The liquid fraction from the separator P 6 is pumped by the pump P 7 , preferably a centrifugal pump, to a pressure between 10 and 20 bar and subsequently combined with the mixed-refrigerant stream compressed in the compressor P 8 .

The mixed refrigerant of the first or PRC mixed-refrigerant cycle is preferably compressed in a two-stage single-casing centrifugal compression apparatus which comprises both the cooler P 4 and the separator P 6 . In the case of very high volumes, instead of the centrifugal compression apparatus, an axial compression apparatus can alternatively be provided.

The compressed mixed refrigerant of the PRC mixed-refrigerant cycle is condensed in the cooler P 9 , preferably against sea water or a corresponding coolant medium, and slightly subcooled to a temperature range of 10 to 40° C. The mixed refrigerant is subsequently fed via line P 10 to the heat exchanger E 1 and subcooled in this against itself to a temperature between −35 and −50° C.

The vaporization temperature which can be achieved according to the Joule-Thomson expansion in the expansion valve P 13 —or alternatively thereto in an expansion turbine—is essentially dependent on the degree of subcooling prior to the expansion and on the vaporization pressure in the temperature range between −38 and −53° C.

The second or LRC mixed-refrigerant cycle serves, as already mentioned at the outset, to liquefy the precooled natural gas stream in line 2 . The mixed refrigerant of this LRC mixed-refrigerant cycle essentially consists of a mixture of 5 to 15 mol % methane, 0 to 80 mol % ethylene or ethane and 10 to 20 mol % propane. The precooled natural gas stream is fed to the heat exchanger E 2 via line 2 , cooled in this to a temperature between −80 and −100° C. and subsequently taken off from the heat exchanger E 2 via line 3 .

The mixed refrigerant of the third or SRC mixed-refrigerant cycle is fed to the heat exchanger E 2 via line S 6 at a temperature between −35 and −50° C. and condensed against the refrigerant of the LRC mixed-refrigerant cycle in line L 10 . The mixed refrigerant in line L 10 vaporizes to a pressure level between 1.5 and 6 bar. The cooled mixed refrigerant of the SRC mixed-refrigerant cycle is taken off from the heat exchanger E 2 via line S 7 at a temperature between −80 and −100° C.

The vaporized and superheated mixed refrigerant of the LRC mixed-refrigerant cycle in the line L 10 is fed to the separator L 1 at a pressure between 1.5 and 6 bar. The gaseous mixed refrigerant produced at the top of the separator L 1 is fed via line L 2 to the compressor L 3 and compressed in this to a pressure between 10 and 20 bar. The compressor E 3 is preferably designed as a single-casing axial or centrifugal compressor. Cold-intake compressors of this type have the advantage that the intake medium does not need to be heated up to ambient temperature prior to intake, which saves heating area and thus the heat exchangers can be made smaller and manufactured more cheaply.

The compressed mixed refrigerant of the LRC mixed-refrigerant cycle is cooled in the cooler L 4 to a temperature between 10 and 40° C., preferably against sea water or a corresponding coolant medium. The mixed refrigerant taken off from the cooler L 4 via line L 5 is, as already mentioned, liquefied in the heat exchanger E 1 , fed via line L 6 to the heat exchanger E 2 and subcooled in this to a temperature between −80 and −100° C. against itself. The vaporization temperature of the mixed refrigerant according to the Joule-Thomson expansion in the expansion valve L 9 —or alternatively thereto in an expansion turbine—is between −82 and −112° C.

The third or SRC mixed-refrigerant cycle serves for subcooling the liquefied hydrocarbon-rich stream or natural gas stream. This subcooling is expedient or necessary in order that no more than the required amount of the flash gas is produced after the expansion of the liquefied hydrocarbon-rich stream in a down-stream nitrogen removal unit.

The mixed refrigerant of the third or SRC mixed-refrigerant cycle, according to a further advantageous development of the process according to the invention, essentially consists of a mixture of 0 to 10 mol % nitrogen, 40 to 65 mol % methane and 0 to 40 mol % ethylene or 0 to 30 mol % ethane.

The liquefied hydrocarbon-rich stream fed to the heat exchanger E 3 via line 3 is subcooled in the heat exchanger E 3 to a temperature of −150 to −160° C. After this subcooling, the hydrocarbon-rich stream or natural gas stream is taken off via line 4 from the heat exchanger E 3 and expanded essentially to atmospheric pressure by means of a Joule-Thomson expansion in expansion valve 5—or alternatively thereto in an expansion turbine.

The mixed refrigerant of the third or SRC mixed-refrigerant cycle fed to the heat exchanger E 3 via line S 9 is subcooled in the heat exchanger E 3 and is subsequently likewise subjected to a Joule-Thomson expansion in expansion valve S 10 . Instead of expansion valve S 10 , again an expansion turbine can be provided. The expansion in expansion valve S 10 is performed to a pressure level between 2 and 6 bar. The vaporization of the mixed refrigerant in heat exchanger E 3 serves both for subcooling the already liquefied hydrocarbon-rich stream and for the self-subcooling of the as yet unexpanded mixed refrigerant of the SRC mixed-refrigerant cycle.

The vaporized and superheated mixed refrigerant of the SRC mixed-refrigerant cycle is fed via line S 11 to a separator S 1 . The gaseous mixed refrigerant produced at the top of the separator S 1 is fed via line S 2 to a compressor S 3 . In compressor S 3 , the mixed refrigerant is compressed to a pressure between 35 and 60 bar. The mixed refrigerant exiting from the compressor S 3 is subsequently cooled in the cooler S 4 , preferably against sea water or a suitable coolant medium.

Each of the three mixed-refrigerant cycles has, in accordance with a further advantageous development of the process according to the invention, a separator/storage vessel P 11 , L 7 or S 8 downstream of the respective expansion valve P 13 , L 9 or S 10 . In principle, these separators/storage vessels can also be provided at any other suitable point of the mixed-refrigerant cycles.

The liquid fraction is taken off via lines P 16 , L 12 or S 13 from these separators/storage vessels P 11 , L 7 and S 8 and fed to the respective vaporous top fraction (flash gas) of the mixed refrigerant. This procedure ensures a good distribution of liquid and gas and thus good heat transfer in the heat exchangers E 1 , E 2 and E 3 , in particular if these are what are known as plate-fin-type heat exchangers.

Control valves P 15 , L 11 and S 12 are provided in lines P 16 , L 12 and S 13 . These control valves serve for regulating the liquid level within the separators/storage vessels P 11 , L 7 or S 8 .

In the event that the plant is shut down, the control valves P 15 , L 11 and S 12 are closed, so that the separators/storage vessels P 11 , L 7 and S 8 are filled with the mixed refrigerant of the respective mixed-refrigerant cycle; for this purpose it is expedient that control valves—which are not shown in the FIGS. 1 to 5 —are additionally provided at the top of the separators/storage vessels P 11 , L 7 and S 8 . This enables the mixed refrigerant to be stored at the coldest point of the respective mixed-refrigerant cycle, as a result of which the start-up procedure is accelerated during reoperation. The separators/storage vessels P 11 , L 7 and S 8 are preferably dimensioned such that they can store the total volume of mixed refrigerant of a mixed-refrigerant cycle.

In a development of the process according to the invention, it is proposed that the compressors P 8 , P 3 , L 3 and S 3 are driven by only one gas turbine drive G; this is shown by the dash-dotted line (note: even if, in FIGS. 3 to 5 , the designations of the compressors or compressor stages are changed with respect to FIGS. 1 and 2 , the dash-dotted line is intended to make it clear that only one compressor drive is required in these developments of the process according to the invention.).

FIG. 2 shows a liquefaction process for natural gas which is essentially identical to that of FIG. 1 . The first, second and third or PRC, LRC and SRC mixed-refrigerant cycles, for the sake of clarity, are shown only in part, however.

The hydrocarbon-rich stream or natural gas stream to be liquefied is fed via line 1 to the heat exchanger E 1 . At an appropriately chosen temperature level, it is taken off via line 1 ′ from the heat exchanger E 1 and fed to a separation column T 1 which has a reboiler R 1 . This separation column T 1 serves to separate off heavy hydrocarbons, which are taken off via line 8 at the bottom of the separation column T 1 .

The natural gas which is depleted in heavy hydrocarbons and arises at the top of the separation column T 1 is in turn fed via line 2 ′ to the heat exchanger E 1 . In this, it is further cooled and fed as part-condensed stream via line 2 ″ to a separator D. The liquid fraction arising at the bottom of the separator D is added as reflux to the top of the separation column T 1 by means of the pump P 1 via line 2 ″′. The hydrocarbon-rich fraction produced at the top of the separator is fed via line 2 to the heat exchanger E 2 and liquefied in this. The liquefied hydrocarbon-rich stream subsequently passes via line 3 to the heat exchanger E 3 , in which it is subcooled.

The subcooled liquefied hydrocarbon-rich stream is subsequently fed via line 4 to the separation column T 2 , it being conducted through the column bottom phase, for the purpose of heating the reboiler R 2 , prior to the expansion in expansion valve 5 .

The separation column T 2 serves for separating off nitrogen and methane, a stream rich in these two components being taken off at the top of the separation column T 2 via line 6 . This nitrogen- and methane-rich stream—known as the tail gas—taken off via line 6 is warmed in heat exchanger E 4 against a partial stream of the hydrocarbon-rich stream which is taken off at the top of the separator D and is fed via line 9 to the heat exchanger E 4 . The hydrocarbon-rich partial stream which is liquefied in the course of this is subsequently likewise added to separation column T 2 via line 10 and expansion valve 11 —either at the same plate or at any plate below the feed point of the hydrocarbon-rich stream in line 4 .

The liquefied and subcooled natural gas taken off from the bottom phase of the separation column T 2 is fed to storage via line 7 by pump P 2 .

FIG. 3 shows a further advantageous development of the process according to the invention. In this embodiment the first or PRC mixed-refrigerant cycle is modified with respect to the embodiment shown in FIG. 1 . The LRC and SRC mixed-refrigerant cycles, in contrast, are identical to those as shown in FIG. 1 .

The compressed (P 3 ) mixed refrigerant is cooled to a temperature between 10 and 40° C. in cooler P 4 and liquefied in the course of this. It is subsequently fed via line P 10 to heat exchanger E 1 and subcooled in this. A partial stream of the subcooled mixed refrigerant is expanded in expansion valve P 13 —or alternatively thereto in an expansion turbine—and vaporized again in heat exchanger E 1 . Subsequently, this mixed-refrigerant partial stream is fed via line P 14 to the separator P 1 at a pressure of 2 to 6 bar. The gaseous mixed refrigerant taken off via line P 2 at the top of separator P 1 is compressed to a pressure between 6 and 10 bar in compressor P 3 .

A second partial stream of the liquefied and subcooled mixed refrigerant is taken off at a higher temperature level from the heat exchanger E 1 and expanded in expansion valve P 17 —or alternatively thereto in an expansion turbine. For the sake of clarity, the separator/storage vessel which can be provided downstream of the expansion valve P 17 and the corresponding control valves are not shown in the figure. After expansion in P 17 , this partial stream of the mixed refrigerant is likewise vaporized in the heat exchanger E 1 and fed via line P 18 to the separator P 6 . The gaseous mixed refrigerant taken off at the top of the separator P 6 via line P 19 is likewise fed to the compressor P 3 at an intermediate pressure stage.

After mixing and compression of the two described mixed-refrigerant partial streams to approximately 15 to 20 bar in the compressor P 3 , the compressed mixed refrigerant is cooled and liquefied in the cooler P 4 at a temperature between 10 and 40° C., preferably against seawater, against air or against an appropriate coolant medium.

This embodiment of the process according to the invention has the advantages and disadvantages below in comparison with the embodiment shown in FIG. 1 :

The enthalpy-temperature diagram of the mixed-refrigerant stream to be vaporized and warmed of the PRC mixed-refrigerant cycle can be adapted better to the enthalpy-temperature diagrams of all streams to be cooled (natural gas stream, PRC, LRC and SRC mixed-refrigerant cycle). The very large gas stream on the suction side of the compressor P 3 is divided into two streams. This requires additional piping and control apparatus. The dimensions of the piping are smaller, however. Overall, the energy consumption of this embodiment of the process according to the invention is lower.

FIGS. 4 and 5 show further advantageous developments of the process according to the invention. In these embodiments, the first or PRC mixed-refrigerant cycle and/or the second or LRC mixed-refrigerant cycle are modified in comparison with the embodiment shown in FIG. 1 . In contrast, the SRC mixed-refrigerant cycle is identical to those shown in FIGS. 1 and 3 . For the sake of clarity, therefore, the SRC mixed-refrigerant cycle is not shown in entirety.

In the case of the embodiment shown in FIG. 4 , in addition, the first or PRC mixed-refrigerant cycle is identical to that shown in FIG. 3 .

The compressed, and subsequently cooled in cooler L 4 to a temperature between 10 and 40° C., mixed refrigerant of the second or LRC mixed-refrigerant cycle is firstly fed via line L 5 to the heat exchanger E 1 and liquefied in this. Subsequently, the mixed refrigerant is fed via line L 6 to the heat exchanger E 2 and subcooled in this. A partial stream of the subcooled mixed refrigerant is expanded in expansion valve L 9 —or alternatively thereto in an expansion turbine—and vaporized in heat exchanger E 2 . This mixed-refrigerant partial stream is subsequently fed via line L 10 to the separator L 1 . The gaseous mixed refrigerant taken off at the top of the separator L 1 via line L 2 is compressed in the compressor L 3 to a pressure between 10 and 20 bar.

A second partial stream of the subcooled mixed refrigerant of the LRC mixed-refrigerant cycle is taken off at a higher temperature level from the heat exchanger E 2 and expanded in the expansion valve L 13 —or alternatively thereto in an expansion turbine. For the sake of clarity, the separator/storage vessel which can be provided downstream of the expansion valve L 13 and the corresponding control valves are not shown in the figure. After expansion in L 13 , this partial stream of the mixed refrigerant is likewise vaporized in heat exchanger E 2 and fed via line L 14 to separator L 15 . The gaseous mixed refrigerant taken off at the top of the separator L 15 via line L 16 is likewise fed to the compressor L 3 at an intermediate pressure stage.

After mixing the two described mixed-refrigerant partial streams in the compressor L 3 , the compressed mixed refrigerant is cooled in cooler L 4 to a temperature between 10 and 40° C., preferably against seawater, against air or against an appropriate coolant medium.

This embodiment of the process according to the invention has the advantages and disadvantages below in comparison with the embodiment shown in FIGS. 1 and 3 :

In this case also, the enthalpy-temperature diagrams of the streams to be cooled and warmed can be better adapted to one another. Whether the energy savings which can be achieved by this embodiment of the process according to the invention justify the extra expenditure for the more complex process procedure and plant must be investigated for each individual case.

In the case of the embodiment of the process according to the invention shown in FIG. 5 , only the second or LRC mixed-refrigerant cycle is modified in comparison with the embodiment shown in FIG. 1 .

The mixed refrigerant which is compressed and subsequently cooled and partially liquefied in cooler L 21 to a temperature between 10 and 40° C. is firstly fed via line L 5 to a separator L 13 . The gaseous fraction of the mixed refrigerant is taken off at the top of the separator L 13 via line L 6 , liquefied in heat exchanger E 1 and subcooled in heat exchanger E 2 . Subsequently, the mixed refrigerant is expanded in expansion valve L 9 —or alternatively thereto in an expansion turbine—and vaporized in heat exchanger E 2 , after which it is fed via line L 10 to the separator L 1 .

The liquid fraction of the mixed refrigerant is taken off from the bottom of the separator L 13 via line L 14 , subcooled in the heat exchanger E 1 and brought to a less low temperature level in the heat exchanger E 2 . Subsequently, this liquefied and subcooled mixed-refrigerant partial stream is expanded in expansion valve L 15 —or alternatively thereto in an expansion turbine—likewise vaporized in heat exchanger E 2 and admixed to the vaporized mixed-refrigerant partial stream in line L 10 . For the sake of clarity, the separator/storage vessel which can be provided downstream of the expansion valve L 15 and the corresponding control valves are not shown in FIG. 5 .

The gaseous mixed refrigerant which is taken off at the top of the separator L 1 via line L 2 is compressed in the compressor L 3 to a pressure between 8 and 10 bar. Subsequently, the compressed mixed refrigerant is cooled in cooler L 4 to a temperature between 10 and 40° C., preferably against seawater, against air or against a suitable coolant medium.

Subsequently thereto, the mixed refrigerant is fed via line L 16 to a further separator L 17 . The gaseous fraction of the mixed refrigerant produced at the top of the separator L 17 is fed via line L 18 to the second compressor stage L 19 and compressed in this to a pressure of between 12 and 25 bar. The liquid fraction from the separator L 17 is pumped to a pressure between 12 and 25 bar by the pump L 20 , preferably a centrifugal pump, and is subsequently combined with the mixed-refrigerant stream compressed in compressor L 19 .

The mixed refrigerant of the second or LRC mixed-refrigerant cycle is preferably compressed in a two-stage single-casing centrifugal compression apparatus which comprises both the cooler L 4 and the separator L 17 . In the case of very high volumes, instead of the centrifugal compression apparatus, an axial compression apparatus can alternatively be provided.

This embodiment of the process according to the invention has the advantages and disadvantages below in comparison with the embodiment shown in FIGS. 1 , 2 and 3 :

In the case of the embodiment of the process according to the invention shown in FIG. 5 , also, the enthalpy-temperature diagrams of the streams to be cooled and warmed can be better adapted to one another. Whether the energy savings which can be achieved by this embodiment justify the additional expenditure for the more complex process procedure or plant must again be investigated for each individual case.

In some circumstances it can be expedient to provide the compressors and drives shown in FIGS. 1 to 5 in a liquefaction plant twice (e.g. 2* 50%). By means of the redundancy resulting from this, even in the event of a fault in one machine, at least 50% of the production is maintained.

Claims

1. A process for liquefying a hydrocarbon-rich stream by indirect heat exchange with the refrigerants of a mixed-refrigerant cascade cycle, wherein the mixed-refrigerant cascade cycle comprises at least 3 mixed-refrigerant cycles having different refrigerant compositions, the first of the 3 mixed-refrigerant cycles serves for precooling (E1), the second mixed-refrigerant cycles serves for liquefying (E2) and the third mixed-refrigerant cycles serves for subcooling (E1) the hydrocarbon-rich stream(1) to be liquefied, characterized in that the mixed-refrigerants are subcooled and either work expanded or subjected to Joule-Thomson expansion, and the resultant cooled gas is heated in indirect heat exchange with said hydrocarbon-rich stream, and the resultant vaporized mixed refrigerants are compressed at temperatures less than ambient temperature by at least two of the three cold-intake compressors (P3, L3, S3) each compressor compressing a different mixed refrigerant.

2. Process for liquefying a hydrocarbon-rich stream according to claim 1, characterized in that the first of the 3 mixed-refrigerant cycles serves for precooling (E1), the second mixed-refrigerant cycle serves for liquefying (E2) and the third mixed-refrigerant cycle serves for subcooling (E3) the hydrocarbon-rich stream (1) to be liquefied.

3. Process for liquefying a hydrocarbon-rich stream according to claims 2, characterized in that the mixed refrigerant of the first of the 3 mixed-refrigerant cycles (P5, P10, . . . ) essentially comprises 0 to 40 mol % ethylene or ethane, 30 to 40 mol % propane and 20 to 30 mol % butane.

4. Process for liquefying a hydrocarbon-rich stream according to 2, characterized in that the mixed refrigerant of the second of the 3 mixed-refrigerant cycles (L5, L6, . . . ) essentially comprises 5 to 15 mol % methane, 0 to 80 mol % ethylene or ethane and 10 to 20 mol % propane.

5. Process for liquefying a hydrocarbon-rich stream according to claim 2, characterized in that the mixed refrigerant of the third of the 3 mixed-refrigerant cycles (S5, S6, . . . ) essentially comprises 0 to 10 mol % nitrogen, 40 to 65 mol % methane and 0 to 40 mol % ethylene or 0 to 30 mol % ethane.

6. Process for liquefying a hydrocarbon-rich stream according to claim 2, characterized in that the precooling (E1), the liquefaction (E2) and the subcooling (E3) of the hydrocarbon-rich stream (1) to be liquefied is performed in at least 3 heat exchangers (E1, E2, E3) and the expanded mixed refrigerant of each of the 3 mixed-refrigerant cycles is fed merely through the last heat exchanger (E1, E2 or E3) prior to the next compression (P3, L3, S3).

7. Process for liquefying a hydrocarbon-rich stream according to claim 1, characterized in that the compressors (P3, L3, S3) used for compressing the mixed refrigerants are driven by only one drive apparatus (G), in particular a gas turbine drive apparatus.

8. Process for liquefying a hydrocarbon-rich stream according to claim 1, characterized in that, in the event of a stoppage of the plant or process, at least the mixed refrigerant of one of the mixed-refrigerant cycles is or are temporarily stored in at least one separator/storage vessel (P11, L7, S8) which is or are preferably arranged at the coldest point of each mixed-refrigerant cycle.

9. Process for liquefying a hydrocarbon-rich stream according to claim 3, characterized in that the mixed refrigerant of the first of the 3 mixed-refrigerant cycles (P5, P10, . . . ) essentially comprises 0 to 40 mol % ethylene or ethane, 30 to 40 mol % propane and 20 to 30 mol % butane.

10. A process for liquefying a hydrocarbon-rich stream according to claim 3, characterized in that the mixed refrigerant of the first of the 5 mixed-refrigerant cycles (P5, P10, . . . ) essentially comprises 0 to 40 mol % ethylene or ethane, 30 to 40 mol % propane and 20 to 30 mol % butane.

11. A process according to claim 1 wherein prior to compression at below ambient temperatures, the expanded mixed refrigerants are passed directly into a separator to provide a vapor depleted of liquid, and the resultant vapor is passed directly to said cold-intake compressor.

12. A process according to claim 1 wherein the hydrocarbon-rich stream is a natural gas stream.

13. A process according to claim 11 wherein the hydrocarbon-rich stream is a natural gas stream.

14. A process according to claim 7 wherein the drive apparatus is a gas turbine gas apparatus.

15. A process according to claim 8 wherein the at least one separator or storage vessel is arranged at the coldest point of each mixed-refrigerant cycles.

16. In a process for liquefying a hydrocarbon-rich stream, by indirect heat exchange with the refrigerants of a mixed-refrigerant cascade cycle, wherein the mixed-refrigerant cascade cycle comprises at least 3 mixed-refrigerant cycles having different refrigerant compositions, the improvement wherein the compressors (P3, L3, S3) used for compressing the mixed refrigerant are driven by only one drive apparatus.

17. A process according to claim 16 wherein drive apparatus is a gas turbine system.

18. A process according to claim 17 wherein the hydrocarbon-rich stream is a natural gas stream.