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    • 专利摘要:
    INTEGRATED PRE-COOLED MIXED REFRIGERANT SYSTEM AND METHOD. The invention relates to a system and method for cooling and liquefying a gas in a heat exchanger that includes compressing and cooling a mixed refrigerant using a first and last compression and cooling cycle so that liquid and vapor flows from high pressure are formed. The high pressure liquid and vapor flows are cooled in the heat exchanger and then expanded so that a primary cooling flow is provided in the heat exchanger. The mixed refrigerant is cooled and balanced between the first and last compression and cooling cycles so that a stream of pre-cooling liquid is formed and subcooled in the heat exchanger. The flow is then expanded and passed through the heat exchanger as a pre-cooling refrigeration flow. A gas flow is passed through the heat exchanger in exchange for countercurrent heat with the primary refrigeration flow and the pre-cooling refrigeration flow so that the gas is cooled.
    公开号:BR112012023457B1
    申请号:R112012023457-9
    申请日:2011-03-04
    公开日:2021-02-02
    发明作者:Tim Gushanas；Doug Douglas Ducote, Jr；James Podolski
    申请人:Chart Inc；
    IPC主号:
    专利说明:

    FIELD OF THE INVENTION
    [0001] The present invention generally relates to processes and systems for cooling or liquefying gases and, more specifically, an improved mixed refrigerant system and method for cooling or liquefying gases. BACKGROUND
    [0002] Natural gas, which is primarily methane, and other gases, are liquefied under pressure for storage and transportation. The reduction in volume that results from liquefaction allows more practical and economical design containers to be used. Liquefaction is typically carried out by cooling the gas through indirect heat exchange for one or more refrigeration cycles, such refrigeration cycles are expensive in terms of both equipment cost and operation due to the complexity of the required equipment and the required performance efficiency. of the soda. There is a need, therefore, for gas cooling and liquefaction systems that have improved cooling efficiency and reduced operating costs with reduced complexity.
    [0003] Liquefying natural gas requires cooling the flow of natural gas to approximately -160 ° C to -170 ° C and then decreasing the pressure to approximately ambient. Figure 1 shows typical temperature curves - enthalpy for methane at 60 bar pressure, methane at 35 bar pressure and a mixture of methane and ethane at 35 bar pressure. There are three regions of the S-shaped curves. Above approximately -75 ° C the gas is no longer overheating and below approximately -90 ° C the liquid is subcooling. The relatively flat intermediate region is where the gas is condensing to a liquid. As the (60 bar) curve is above the critical pressure, there is only one phase present; but its specific heat is great close to the critical temperature, and the cooling curve is similar to the lower pressure curves. The curve containing 5% ethane shows the effect of impurities which round off the dew and boiling points.
    [0004] A cooling process is necessary to supply the cooling to liquefy natural gas, and the most efficient processes will have heating curves which closely approximate the cooling curves in figure 1 to within a few degrees across the entire entire track. However, due to the S-shape of the cooling curves and the wide temperature range, such a cooling process is difficult to design. Due to their vaporization curves, pure component refrigerant processes work best in the two-phase region, but not because of their sloping vaporization curves, multi-component refrigerant processes are more appropriate for regions to stop being overheated and the sub-cooling regions. Both processes, and hybrids of the two, were developed to liquefy natural gas.
    [0005] Pure multi-level cascade component cycles were initially used with refrigerants such as propylene, ethylene, methane, and nitrogen. With sufficient levels, such cycles can generate a liquid heating curve which approximates the cooling curves shown in figure 1. However, the mechanical complexity becomes overwhelming as additional compressor trains are required as the number of levels increases . Such processes are also thermodynamically inefficient because pure component refrigerants vaporize at a constant temperature instead of following the natural gas cooling curve and the refrigeration valve irreversibly flashes the liquid in vapor. For these reasons, improved processes have been pursued in order to reduce the cost of capital, reduce energy consumption and improve operability.
    [0006] US Patent No. 5,746,066 to Manley describes a cascade mixed multi-level refrigerant process as applied to similar refrigeration demands for ethylene recovery which eliminates the thermodynamic inefficiencies of the pure cascade component process. multiple levels. This is because refrigerants vaporize at rising temperatures following the gas cooling curve and the liquid refrigerant is subcooled before flashing thereby reducing thermodynamic irreversibility. In addition, the mechanical complexity is slightly less because only two different refrigerant cycles are required instead of the three or four required for pure refrigerant processes. U.S. Patent Numbers 4,525,185 to Newton; 4,545,795 to Liu et al .; 4,689,063 to Paradowski et al. and 6,041,619 for Fischer et al. all show variations on this topic applied to the liquefaction of natural gas as do U.S. Patent Application Publications Numbers 2007/0227185 to Stone et al. and 2007/0283718 to Hulsey et al.
    [0007] The multi-level cascade mixed refrigerant process is the most efficient known, but a simpler, more efficient process which can be more easily operated is desirable for most plants.
    [0008] U.S. Patent Number 4,033,735 to Swenson describes a single mixed refrigerant process which requires only one compressor for the refrigeration process and which further reduces mechanical complexity. However, for primarily two reasons, the process consumes slightly more energy than the cascade mixed refrigerant process, at the multiple levels discussed above.
    [0009] First, it is difficult, if not impossible, to find a unique mixed refrigerant composition which will generate a liquid heating curve that closely follows the typical natural gas cooling curves shown in figure 1. Such a refrigerant must consist of a range of high and low boiling components, and their boiling temperatures are thermodynamically constrained by phase equilibrium. In addition, the highest boiling components are limited because they must not freeze at the lowest temperatures. For these reasons, relatively large temperature differences necessarily occur at various points in the cooling process. Figure 2 shows the typical compound heating and cooling curves for the Swenson '735 patent process.
    [00010] Second, for the single mixed refrigerant process, all components in the refrigerant are charged to the lowest temperature level even though the highest boiling components only provide refrigeration at the hottest end of the refrigerated portion of the process. This requires energy to cool and reheat these components which are "inert" at the lowest temperatures. This is not the case with the multi-level cascade pure component cooling process or the multi-level cascade mixed refrigerant process.
    [00011] To mitigate this second inefficiency and also solve the first, numerous solutions have been developed which separate a heavier fraction from a single mixed refrigerant, use the heavier fraction at the highest refrigeration temperature levels, and then recombine it with the lightest fraction for subsequent compression. U.S. Patent Number 2,041,725 to Podbielniak describes a way of doing this which incorporates several stages of phase separation at temperatures below ambient. U.S. Patent Numbers 3,364,685 to Perret; 4,057,972 to Sarsten; 4,274,849 to Garrier et al .; 4,901,533 to Fan et al .; 5,644,931 to Ueno et al .; 5,813,250 to Ueno et al .; 6,065,305 to Arman et al .; 6,347,531 to Roberts et al. and U.S. Patent Application Publication 2009/0205366 to Schmidt also show variations on this topic. When carefully designed, they can improve energy efficiency even though the recombination of unbalanced flows is thermodynamically inefficient. This is because the light and heavy fractions are separated at high pressure and then recombined at low pressure so that they can be compressed together in the single compressor. Whenever the flows are separated in equilibrium, separately processed and then recombined in conditions of non-equilibrium, a thermodynamic loss occurs which in the end increases energy consumption. Therefore, the number of such separations should be minimized. All of these processes use a simple vapor / liquid balance at various locations in the refrigeration process to separate the heavier from the lighter fraction.
    [00012] Single-stage vapor / liquid equilibrium separation, however, does not concentrate fractions as much as can be performed using multiple reflux equilibrium stages. A higher concentration allows greater precision in isolating a composition which will provide cooling over a specific temperature range. This improves the process ability to follow the S-shaped cooling curves in figure 1. U.S. Patent Numbers 4,586,942 to Gauthier and 6,334,334 to Stockman et al. describe how fractionation can be used in the above-air compressor train to additionally concentrate the separate fractions used for refrigeration in different temperature zones and thus improve the total process thermodynamic efficiency. A second reason for concentrating the fractions and reducing their vaporization temperature range is to ensure that they are completely vaporized when they leave the refrigerated part of the process. This makes full use of the latent heat of the refrigerant and prevents liquids from being drawn into downstream compressors. For this same reason, heavy fraction liquids are normally reinjected into the lighter fraction of the refrigerant as part of the process. The fractionation of the heavy fraction reduces flashing upon reinjection and improves the mechanical distribution of the two-phase fluids.
    [00013] As illustrated by U.S. Patent Application Publication Number 2007/0227185 to Stone et al., It is known to remove partially vaporized refrigeration streams from the refrigerated portion of the process. Stone et al. it does this for mechanical (non-thermodynamic) reasons and in the context of a multi-level cascade mixed refrigerant process that requires two separate, mixed refrigerants. In addition, partially vaporized cooling streams are completely vaporized upon recombination with their vapor fractions previously separated immediately before compression. BRIEF DESCRIPTION OF THE DRAWINGS
    [00014] Figure 1 is a graphical representation of temperature curves - enthalpy for methane at pressures of (35 bar and 60 bar) and a mixture of methane and ethane at a pressure of (35 bar); figure 2 is a graphical representation of the heating and cooling curves composed for a prior art process and system; figure 3 is a flowchart and process diagram illustrating an embodiment of the process and system of the invention; figure 4 is a graphical representation of heating and cooling curves composed for the process and system of figure 3; figure 5 is a flow chart and process diagram illustrating a second embodiment of the process and system of the invention; figure 6 is a flow chart and process diagram illustrating a third embodiment of the process and system of the invention; figure 7 is a flow diagram and process diagram illustrating a fourth embodiment of the process and system of the invention; figure 8 is a graphical representation that provides enlarged views of the hot end portions of the heating and cooling curves composed of figures 2 and 4; DETAILED DESCRIPTION OF MODALITIES
    [00015] According to the invention, and as explained in greater detail below, a simple equilibrium separation of a heavy fraction is sufficient to significantly improve the efficiency of the mixed refrigerant process if this heavy fraction is not entirely vaporized as it leaves the primary process heat exchanger. This means that some liquid refrigerant will be present in the compressor suction and must be separated and pumped in advance to a higher pressure. When the liquid refrigerant is mixed with the lighter vaporized fraction of the refrigerant, the compressor suction gas is greatly cooled and the required compressor power is further reduced. Balancing separation of the heavy fraction during an intermediate stage also reduces the load on the second or higher stage compressor (s), resulting in improved process efficiency. Heavy refrigerant components are also kept out of the cold end of the process, reducing the possibility of refrigerant freezing.
    [00016] Furthermore, the use of the heavy fraction in an independent pre-cooling refrigeration loop results in the heating / cooling curves being almost closed at the hot end of the heat exchanger, providing a more efficient use of refrigeration. This is best illustrated in figure 8 where the curves in figures 2 (open curves) and 4 (closed curves) are drawn on the same geometric axes with the temperature range limited to + 40 ° C to -40 ° C.
    [00017] A flowchart and process diagram illustrating a modality of the system and method of the invention is provided in figure 3. The operation of the modality will now be described with reference to figure 3.
    [00018] As illustrated in the figure, the system includes a multi-flow heat exchanger, generally indicated at 6, which has a hot end 7 and a cold end 8. The heat exchanger receives a natural gas supply stream of high pressure 9 which is liquefied in the cooling passage 5 by removing heat through heat exchange with the cooling flows in the heat exchanger. As a result, a stream 10 of a liquid natural gas product is produced. The multi-flow design of the heat exchanger allows for convenient and energy-efficient integration of multiple flows into a single exchanger. Suitable heat exchangers can be purchased from Chart Energy & Chemicals, Inc. of The Woodlands, Texas. The multi-plate plate and fin heat exchanger available from Chart Energy & Chemicals, Inc. offers the added advantage of being physically compact.
    [00019] The system of figure 3, including the heat exchanger 6, can be configured to perform other gas processing options, indicated in dashes in 13, known in the prior art. These processing options may require the gas flow to exit and re-enter the heat exchanger one or more times and may include, for example, recovery of natural gas liquids or nitrogen rejection. Furthermore, although the system and method of the present invention are described below in terms of liquefaction of natural gas, they can be used for the cooling, liquefaction and / or processing of gases other than natural gas including, but not limited to, air or nitrogen.
    [00020] Heat removal is performed on the heat exchanger using a single mixed refrigerant and the remaining portion of the system illustrated in figure 3. The refrigerant compositions, conditions and current flows of the refrigeration portion of the system, as described below , are shown in Table 1.
    [00021] With reference to the upper right portion of figure 3, a first stage compressor 11 receives a flow of low pressure steam refrigerant 12 and compresses it to an intermediate pressure. Flow 14 then moves to a first stage post-cooler 16 where it is cooled. The post-cooler 16 can, as an example, be a heat exchanger. The resulting intermediate pressure mixed phase refrigerant flow 18 moves to the interstage drum 22. Although an interstage drum 22 is illustrated, alternative separation devices can be used, including, but not limited to, another type of reservoir , cyclonic separator, distillation unit, a coalescent separator or mist eliminator of the type of screen or fin. The interstage drum 22 also receives a flow of intermediate pressure liquid refrigerant 24, which, as will be explained in more detail below, is provided by pump 26. In an alternative embodiment, flow 24 can instead combine with flow 14 upstream of the post-cooler 16 or flow 18 downstream of the post-cooler 16.
    [00022] Flows 18 and 24 are combined and balanced within the interstage drum 22 which results in a separate intermediate pressure vapor stream 28 exiting the vapor outlet of drum 22 and an intermediate pressure liquid stream 32 which comes out of the liquid outlet of the drum. The intermediate pressure liquid flow 32, which is hot and a heavy fraction, leaves the liquid side of the drum 22 and enters the pre-cooling liquid passage 33 of the heat exchanger 6 and is subcooled by the heat exchanger with the various cooling flows, described below, which also pass through the heat exchanger. The resulting flow 34 exits the heat exchanger and is flashed through expansion valve 36. As an alternative to expansion valve 36, another type of expansion device could be used, including, but not limited to, a turbine or an orifice . The resulting flow 38 re-enters heat exchanger 6 to provide additional cooling through the pre-cooling refrigeration passage 39. Flow 42 exits the hot end 7 of the heat exchanger as a two-phase mixture with a significant liquid fraction.
    [00023] The intermediate pressure steam stream 28 moves from the steam outlet of the drum 22 to the second or last stage compressor 44 where it is compressed to a high pressure. Flow 46 exits compressor 44 and travels through the second or last stage post-cooler 48 where it is cooled. The resulting flow 52 contains both the vapor and liquid phase which are separated in the accumulator drum 54. Although an accumulator drum 54 is illustrated, alternative separation devices can be used, including, but not limited to, another type of reservoir, a cyclonic separator, distillation unit, a coalescent separator or mist eliminator of the type of screen or fin. The high pressure steam refrigerant flow 56 exits the steam outlet of the drum 54 and moves to the hot side of the heat exchanger 6. The high pressure liquid refrigerant flow 58 exits the liquid outlet of the drum 54 and also moves to the hot end of the heat exchanger 6. It should be noted that the first stage compressor 11 and the first stage cooler 16 comprise a first compression and cooling cycle while the last stage compressor 44 and the powder -48 stage last cooler make up a final compression and cooling cycle. It should also be noted, however, that each cooling cycle stage could alternatively feature multiple compressors and / or post-coolers.
    [00024] The hot, high-pressure refrigerant stream 56 is cooled, condensed and sub-cooled as it travels through the high-pressure passage 59 of the heat exchanger 6. As a result, a stream 62 comes out from the hot end of the heat exchanger 6. Flow 62 is flashed through expansion valve 64 and re-enters the heat exchanger as flow 66 to provide refrigeration as flow 67 that moves through primary refrigeration passage 65. As a As an alternative to expansion valve 64, another type of expansion device could be used, including, but not limited to, a turbine or an orifice.
    [00025] The high pressure liquid refrigerant flow 58 enters the heat exchanger 6 and subcooled inside the high pressure liquid passage 69. The resulting flow 68 leaves the heat exchanger and is flashed through the expansion valve 72. As an alternative to expansion valve 72, another type of expansion device could be used, including, but not limited to, a turbine or an orifice. The resulting flow 74 re-enters heat exchanger 6 where it joins and is combined with flow 67 within primary cooling passage 65 to provide additional cooling like flow 76 and exits the hot end of heat exchanger 6 as a flow superheated steam 78.
    [00026] Superheated steam flow 78 and flow 42 which, as noted above, is a mixture of two phases with a significant liquid fraction, enters the low pressure suction drum 82 through steam and mixed phase inlets. , respectively, and are combined and balanced within the low pressure suction drum. Although a suction drum 82 is illustrated, alternative separation devices can be used, including, but not limited to, another type of reservoir, a cyclonic separator, a distillation unit, a coalescing separator or a mist eliminator of the type mesh or fin. As a result, a flow of low pressure steam refrigerant 12 exits the steam outlet of drum 82. As stated above, flow 12 moves to the inlet of the first stage compressor 11. The mixed phase flow mixture 42 as flow 78, which includes a steam of vastly different composition, within the suction drum 82 at the suction inlet of the compressor 11 creates a partial flash cooling effect that decreases the temperature of the vapor flow traveling to the compressor, and so from the compressor itself, and this reduces the power required to operate it.
    [00027] A low pressure liquid refrigerant flow 84, which has also been decreased in temperature by the flashing cooling effect of the mixture, leaves the liquid outlet of drum 82 and is pumped to an intermediate pressure by pump 26. As above described, the outlet flow 24 of the pump moves to the interstage drum 22.
    [00028] As a result, according to the invention, a pre-cooling refrigerant loop, which includes flows 32, 34, 38 and 42, enters the hot side of the heat exchanger 6 and leaves with a liquid fraction significant. The partially liquid flow 42 is combined with the refrigerant vapor consumed from flow 78 for equilibrium and separation within the suction drum 82, compression of the resulting vapor in the compressor 11 and pumping of the resulting liquid through the pump 26. The balance within the suction drum 82 reduces the temperature of the flow that enters the compressor 11 by both heat and mass transfer, thereby reducing the compressor's use of power.
    [00029] The heating and cooling curves composed of the process in figure 3 are shown in figure 4. A comparison with the curves in figure 2 for a single, optimized mixed refrigerant process, similar to that described in US Patent No. 4,033,735 for Swenson, shows that the composite heating and cooling curves were brought closer together thus reducing the compressor power by approximately 5%. This helps to reduce the cost of capital for a plant and reduces energy consumption with associated environmental emissions. These benefits can result in savings of several million dollars a year for a small to medium size liquid natural gas plant.
    [00030] Figure 4 also illustrates that the system and method of figure 3 results in the close closure of the hot end of the heat exchanger of the cooling curves (see also figure 8). This is because the medium pressure heavy fraction liquid boils at a higher temperature than the rest of the refrigerant and is thus well suited for cooling the hot-end heat exchanger. Boiling the medium pressure heavy fraction liquid separately from the lighter fraction refrigerant in the heat exchanger allows for an even higher boiling temperature, resulting in an even more "closed" (and thus more efficient) hot end of the curve . Furthermore, keeping the heavy fraction off the cold end of the heat exchanger helps to prevent freezing from occurring.
    [00031] It should be noted that the modality described above is for a representative natural gas supply at supercritical pressure. The refrigerant composition and optimal operating conditions will change when liquefying other, less pure, natural gases at different pressures. The advantages of the process remain, however, due to its thermodynamic efficiency.
    [00032] A process and scheme flowchart illustrating a second embodiment of the system and method of the invention is provided in figure 5. In the embodiment of figure 5, the superheated steam flow 78 and the two-phase mixed flow 42 are combined in one mixing device, indicated at 102, instead of the suction drum 82 of figure 3. The mixing device 102 can be, for example, a static mixer, a single tube segment within which flows 78 and 42 flow, a seal or a heat exchanger head 6. After leaving the mixing device 102, the combined and mixed flows 78 and 42 move as a flow 106 to a single inlet of the low pressure suction drum 104. Despite a suction 104 is illustrated, alternative separation devices may be used, including, but not limited to, another type of reservoir, cyclonic separator, distillation unit, a coalescent separator or mist eliminator of the screen or fin type. When flow 106 enters suction drum 104, the vapor and liquid phases are separated so that a low pressure liquid refrigerant flow 84 exits the liquid outlet of drum 104 while a low pressure vapor flow 12 exits. from the steam outlet of the drum 104, as described above for the embodiment of figure 3. The remaining portion of the embodiment of figure 5 has the same components and operation as described for the embodiment of figure 3, although the data in Table 1 may differ.
    [00033] A flowchart and process diagram illustrating a third mode of the system is the method of the invention is provided in figure 6. In the embodiment of figure 6, the mixed two-phase flow 42 of the heat exchanger 6 moves to the return 120. The resulting steam phase moves as the return steam stream 122 to a first steam inlet from the low pressure suction drum 124. The superheated steam flow 78 from the heat exchanger 6 moves to a second inlet of low pressure suction drum 124. The combined flow 126 exits the steam outlet of the suction drum 124. Drums 120 and 124 can alternatively be combined into a single drum or reservoir that performs the functions of the separation drum return and suction drum. Furthermore, alternative types of separation devices can be replaced for drums 120 and 124, including, but not limited to, another type of reservoir, cyclonic separator, distillation unit, a coalescent separator or screen-type mist eliminator or fin.
    [00034] A first stage compressor 131 receives the low pressure vapor refrigerant flow 126 and compresses it to an intermediate pressure. The compressed flow 132 then moves to a first stage post-cooler 134 where it is cooled. Meanwhile, the liquid from the liquid outlet of the return separator drum 120 moves as the return liquid flow 136 to the pump 138, and the resulting flow 142 then joins flow 132 upstream of the first stage aftercooler 134 .
    [00035] The intermediate pressure mixed phase refrigerant flow 144 that leaves the first stage cooler 134 moves to the interstage drum 146. Although an interstage drum 146 is illustrated, alternative separation devices can be used , including, but not limited to, another type of reservoir, cyclonic separator, distillation unit, a coalescent separator or mist eliminator of the screen or fin type. A separate intermediate pressure vapor stream 28 exits the vapor outlet of the interstage drum 146 and an intermediate pressure liquid stream 32 exits the liquid outlet of the drum. The intermediate pressure steam stream 28 moves to the second stage compressor 44, while the intermediate pressure liquid stream 32, which is a hot and heavy fraction, moves to the heat exchanger 6, as described above with respect to the modality of figure 3. The remaining portion of the modality of figure 6 presents the same components and operation as described for the modality of figure 3, although the data in Table 1 may differ. The embodiment of figure 6 does not provide any cooling in drum 124, and thus no cooling of the suction flow of first stage compressor 126. In terms of improving efficiency, however, the suction flow of cold compressor is exchanged for a fee of reduced steam molar flow for compression suction. The reduced steam flow for the compressor suction provides a reduction in the compressor power requirement that is approximately equivalent to the reduction provided by the cooled compressor suction flow of the modality of figure 3. Although there is an associated increase in the power requirement of the compressor. pump 138, compared to pump 26 in the mode of figure 3, the increase in pump power is very small (approximately 1/100) compared to the savings in compressor power.
    [00036] In a fourth embodiment of the system and method of the invention, illustrated in figure 7, the system in figure 3 is optionally provided with one or more pre-cooling systems, indicated in 202, 204 and / or 206. Of course, the modalities of figures 5 or 6, or any other modality of the system of the invention, could be provided with the pre-cooling systems of figure 7. The pre-cooling system 202 is for pre-cooling the flow of natural gas 9 before of the heat exchanger 6. The pre-cooling system 204 is for pre-cooling interstages of the mixed phase flow 18 as it travels from the first stage post-cooler 16 to the interstage drum 22. The pre-cooling system - cooling 206 is for the pre-cooling of the discharge of the mixed phase flow 52 as it moves to the accumulator drum 54 of the second stage post-cooler 48. The remaining portion of the embodiment of figure 7 has the same components and operation as described for for the modality of figure 3, although the data in Table 1 may differ.
    [00037] Each of the 202, 204 or 206 pre-cooling systems could be incorporated or based on the heat exchanger 6 for operation or could include a cooler that could be, for example, a second multi-flow heat exchanger . In addition, two or all three of the 202, 204 and / or 206 pre-cooling systems could be incorporated into a single multi-flow heat exchanger. Although any pre-cooling system known in the art can be used, the pre-cooling systems in figure 7 each preferably include a cooler that uses a single component refrigerant, such as propane, or a second mixed refrigerant as the pre-cooling system refrigerant. More specifically, the well-known C3-MR propane pre-cooling process or dual mixed refrigerant processes, with the pre-cooling refrigerant evaporated at either a single pressure or multiple pressures, could be used. Examples of other suitable single component refrigerants include, but are not limited to, N-butane, iso-butane, propylene, ethane, ethylene, ammonia, freon, or water.
    [00038] In addition to being provided with a pre-cooling system 202, the system of figure 7 (or any of the other system modalities) could serve as a pre-cooling system for a downstream process, such as a system of liquefaction or a second mixed refrigerant system. The gas being cooled in the cooling pass of the heat exchanger could also be a second mixed refrigerant or a single component mixed refrigerant.
    [00039] Although the preferred embodiments of the invention have been shown and described, it will be apparent to those skilled in the art that changes and modifications can be made here without departing from the spirit of the invention, the scope of which is defined by the appended claims. Table 1: Flow Table
    Mol Porcento

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    权利要求:
    Claims (20)
    [0001]
    1. A system for cooling a gas with a mixed refrigerant, comprising: a) a heat exchanger that includes a hot end and a cold end, the hot end having a supply gas inlet adapted to receive a gas supply and the cold end having a product outlet through which the product exits the heat exchanger, said heat exchanger also including a cooling passage in communication with the supply gas inlet and the product outlet, a pre-liquid passage - cooling, a pre-cooling refrigeration passage, a high pressure passage and a primary refrigeration passage; b) a suction separation device that has a steam outlet; c) a first stage compressor that has a suction inlet in fluid communication with the vapor outlet of the suction separation device and an outlet; d) a first stage aftercooler that has an inlet in fluid communication with the outlet of the first stage compressor and an outlet; e) an interstage separation device that has an inlet in fluid communication with the outlet of the first stage post-cooler and that has a vapor outlet in fluid communication with the high pressure passage of the heat exchanger and an outlet of liquid in fluid communication with the passage of pre-cooling liquid from the heat exchanger; f) a first expansion device that has an inlet in fluid communication with the passage of pre-cooling liquid from the heat exchanger and an outlet in communication with the pre-cooling refrigeration passage of the heat exchanger; g) a second expansion device that has an inlet in fluid communication with the high pressure passage of the heat exchanger and an outlet in communication with the primary cooling passage of the heat exchanger; h) said pre-cooling refrigeration passage adapted to produce a mixed phase flow and said primary refrigeration passage adapted to produce a vapor flow; characterized by the fact that it further comprises: i) a mixing device, said mixing device having a vapor input in fluid communication with the primary cooling passage of the heat exchanger and a mixed phase input in communication with the passage of pre-cooled refrigeration of the heat exchanger, so that the steam flow from the primary refrigeration passage and the mixed phase current from the pre-cooled refrigeration passage are combined and mixed in the mixing device, said mixing device also having an output in communication with the input of the suction separation device, so that the combined and mixed currents are supplied to the suction separation device; and j) a pump having an inlet in fluid communication with the liquid outlet of the suction separation device and an outlet configured to by-pass the first stage post-cooler and direct the liquid to the separation device between stages.
    [0002]
    2. System according to claim 1, characterized by the fact that said separation device between stages is adapted to produce a liquid stream containing a heavy fraction of the refrigerant.
    [0003]
    3. System according to claim 1, characterized by the fact that the cooling passage and the high pressure passage pass through the hot and cold ends of the heat exchanger.
    [0004]
    4. System according to claim 1, characterized by the fact that the gas is natural gas.
    [0005]
    5. System according to claim 4, characterized by the fact that the product is liquefied natural gas.
    [0006]
    6. System according to claim 1, characterized by the fact that the product is liquefied gas.
    [0007]
    7. System according to claim 1, characterized by the fact that it also comprises a first pre-cooling system adapted to receive and cool the gas supply and direct the cooled gas to the gas supply inlet of the heat exchanger.
    [0008]
    8. System according to claim 7, characterized by the fact that the first pre-cooling system uses a single component refrigerant as a pre-cooling system refrigerant.
    [0009]
    9. System according to claim 8, characterized by the fact that the single component refrigerant is propane.
    [0010]
    10. System according to claim 7, characterized by the fact that the first pre-cooling system uses a second mixed refrigerant as a pre-cooling system refrigerant.
    [0011]
    11. System according to claim 7, characterized by the fact that it also comprises a second pre-cooling system in the circuit between the output of the first stage compressor and the input of the interstage separation device.
    [0012]
    12. System according to claim 11, characterized by the fact that the first and the second pre-cooling systems are included in a single pre-cooling system using a single pre-cooled refrigerant.
    [0013]
    13. System according to claim 1, characterized by the fact that it also comprises a pre-cooling system in the circuit between the output of the first stage compressor and the input of the interstage separation device.
    [0014]
    14. System according to claim 13, characterized by the fact that the pre-cooling system includes a single component refrigerant such as the pre-cooling system refrigerant.
    [0015]
    15. System according to claim 14, characterized by the fact that the single component refrigerant is propane.
    [0016]
    16. System according to claim 1, characterized by the fact that the mixing device includes a pipe segment.
    [0017]
    17. System according to claim 1, characterized by the fact that the mixing device includes a heat exchanger head.
    [0018]
    18. System according to claim 1, characterized by the fact that the output of the first expansion device is configured to supply a mixed phase current directly to the pre-cooled refrigeration passage of the heat exchanger.
    [0019]
    19. System according to claim 1, characterized by the fact that the separation device between stages has a vapor inlet in fluid communication with the outlet of the first stage after the chiller and a liquid inlet in fluid communication with the outlet the pump.
    [0020]
    20. System according to claim 1, characterized by the fact that the high pressure passage of the heat exchanger is a passage of high pressure steam and in which the heat exchanger also includes a passage of high pressure liquid and further comprising: k) a second stage compressor having a suction inlet in fluid communication with the vapor outlet of the separation device between stages and an outlet; l) a second stage second cooling post having an input in fluid communication with the compressor output of the second stage and an output; m) a high pressure accumulator having a high pressure accumulator input in fluid communication with the outlet of the second stage of the post-cooler, said high pressure accumulator with a high pressure steam outlet and a liquid outlet of high pressure where the high pressure steam outlet is in fluid communication with the high pressure vapor passage of the heat exchanger and the high pressure liquid outlet is in fluid communication with the high pressure liquid passage of the heat exchanger heat; n) a third expansion device having an inlet in fluid communication with the passage of high pressure liquid from the heat exchanger and an outlet in communication with the primary cooling passage of the heat exchanger.
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    法律状态:
    2019-01-08| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2019-10-29| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2020-08-04| B06A| Patent application procedure suspended [chapter 6.1 patent gazette]|
    2020-10-06| B06A| Patent application procedure suspended [chapter 6.1 patent gazette]|
    2020-12-15| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2021-02-02| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 04/03/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US12/726,142|US9441877B2|2010-03-17|2010-03-17|Integrated pre-cooled mixed refrigerant system and method|
    US12/726,142|2010-03-17|
    PCT/US2011/027162|WO2011115760A1|2010-03-17|2011-03-04|Integrated pre-cooled mixed refrigerant system and method|
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