Patent Application
20200318872
The present invention generally relates to mixed refrigerant systems and methods suitable for cooling fluids such as natural gas.
Natural gas and other gases are liquefied for storage and transport. Liquefaction reduces the volume of the gas and is typically carried out by chilling the gas through indirect heat exchange in one or more refrigeration cycles. The refrigeration cycles are costly because of the complexity of the equipment and the performance efficiency of the cycle. There is a need, therefore, for gas cooling and/or liquefaction systems that are less complex, more efficient, and less expensive to operate.
Liquefying natural gas, which is primarily methane, typically requires cooling the gas stream to approximately −160° C. to −170° C. and then letting down the pressure to approximately atmospheric. Typical temperature-enthalpy curves for liquefying gaseous methane, such as shown in
Refrigeration processes supply the requisite cooling for liquefying natural gas, and the most efficient of these have heating curves that closely approach the cooling curves in
Cascaded, multilevel, pure component refrigeration cycles were initially used with refrigerants such as propylene, ethylene, methane, and nitrogen. With enough levels, such cycles can generate a net heating curve that approximates the cooling curves shown in
U.S. Pat. No. 5,746,066 to Manley describes a cascaded, multilevel, mixed refrigerant process for ethylene recovery, which eliminates the thermodynamic inefficiencies of the cascaded multilevel pure component process. This is because the refrigerants vaporize at rising temperatures following the gas cooling curve, and the liquid refrigerant is subcooled before flashing thus reducing thermodynamic irreversibility. Mechanical complexity is somewhat reduced because fewer refrigerant cycles are required compared to pure refrigerant processes. See, e.g., U.S. Pat. No. 4,525,185 to Newton; U.S. Pat. No. 4,545,795 to Liu et al.; U.S. Pat. No. 4,689,063 to Paradowski et al.; and U.S. Pat. No. 6,041,619 to Fischer et al.; and U.S. Patent Application Publication Nos. 2007/0227185 to Stone et al. and 2007/0283718 to Hulsey et al.
The cascaded, multilevel, mixed refrigerant process is among the most efficient known, but a simpler, more efficient process, which can be more easily operated, is desirable.
A single mixed refrigerant process, which requires only one compressor for refrigeration and which further reduces the mechanical complexity has been developed. See, e.g., U.S. Pat. No. 4,033,735 to Swenson. However, for primarily two reasons, this process consumes somewhat more power than the cascaded, multilevel, mixed refrigerant processes discussed above.
First, it is difficult, if not impossible, to find a single mixed refrigerant composition that generates a net heating curve that closely approximates the typical natural gas cooling curve. Such a refrigerant requires a range of relatively high and low boiling components, whose boiling temperatures are thermodynamically constrained by the phase equilibrium. Higher boiling components are further limited in order to avoid their freezing out at low temperatures. The undesirable result is that relatively large temperature differences necessarily occur at several points in the cooling process, which is inefficient in the context of power consumption.
Second, in single mixed refrigerant processes, all of the refrigerant components are carried to the lowest temperature even though the higher boiling components provide refrigeration only at the warmer end of the process. The undesirable result is that energy must be expended to cool and reheat those components that are “inert” at the lower temperatures. This is not the case with either the cascaded, multilevel, pure component refrigeration process or the cascaded, multilevel, mixed refrigerant process.
To mitigate this second inefficiency and also address the first, numerous solutions have been developed that separate a heavier fraction from a single mixed refrigerant, use the heavier fraction at the higher temperature levels of refrigeration, and then recombine the heavier fraction with the lighter fraction for subsequent compression. See, e.g., U.S. Pat. No. 2,041,725 to Podbielniak; U.S. Pat. No. 3,364,685 to Perret; U.S. Pat. No. 4,057,972 to Sarsten; U.S. Pat. No. 4,274,849 to Garrier et al.; U.S. Pat. No. 4,901,533 to Fan et al.; U.S. Pat. No. 5,644,931 to Ueno et al.; U.S. Pat. No. 5,813,250 to Ueno et al; U.S. Pat. No. 6,065,305 to Arman et al., and U.S. Pat. No. 6,347,531 to Roberts et al.; and U.S. Patent Application Publication No. 2009/0205366 to Schmidt. With careful design, these processes can improve energy efficiency even though the recombining of streams not at equilibrium 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 may be compressed together in a single compressor. Generally, when streams are separated at equilibrium, separately processed, and then recombined at non-equilibrium conditions, a thermodynamic loss occurs, which ultimately increases power consumption. Therefore the number of such separations should be minimized. All of these processes use simple vapor/liquid equilibrium at various places in the refrigeration process to separate a heavier fraction from a lighter one.
Simple one-stage vapor/liquid equilibrium separation, however, doesn't concentrate the fractions as much as using multiple equilibrium stages with reflux. Greater concentration allows greater precision in isolating a composition that provides refrigeration over a specific range of temperatures. This enhances the process ability to follow the typical gas cooling curves. U.S. Pat. No. 4,586,942 to Gauthier and U.S. Pat. No. 6,334,334 to Stockmann et al (the latter marketed by Linde as the LIMUM®3 process) describe how fractionation may be employed in the above ambient compressor train to further concentrate the separated fractions used for refrigeration in different temperature zones and thus improve the overall process thermodynamic efficiency. A second reason for concentrating the fractions and reducing their temperature range of vaporization is to ensure that they are completely vaporized when they leave the refrigerated part of the process. This fully utilizes the latent heat of the refrigerant and precludes the entrainment of liquids into downstream compressors. For this same reason heavy fraction liquids are normally re-injected into the lighter fraction of the refrigerant as part of the process. Fractionation of the heavy fractions reduces flashing upon re-injection and improves the mechanical distribution of the two phase fluids.
As illustrated by U.S. Patent Application Publication No. 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. does this for mechanical (and not thermodynamic) reasons and in the context of a cascaded, multilevel, mixed refrigerant process that requires two separate mixed refrigerants. The partially vaporized refrigeration streams are completely vaporized upon recombination with their previously separated vapor fractions immediately prior to compression.
Multi-stream, mixed refrigerant systems are known in which simple equilibrium separation of a heavy fraction was found to significantly improve the mixed refrigerant process efficiency if that heavy fraction isn't entirely vaporized as it leaves the primary heat exchanger. See, e.g., U.S. Patent Application Publication No. 2011/0226008 to Gushanas et al. Liquid refrigerant, if present at the compressor suction, must be separated beforehand and sometimes pumped to a higher pressure. When the liquid refrigerant is mixed with the vaporized lighter fraction of the refrigerant, the compressor suction gas is cooled, which further reduces the power required. Heavy components of the refrigerant are kept out of the cold end of the heat exchanger, which reduces the possibility of refrigerant freezing. Also, equilibrium separation of the heavy fraction during an intermediate stage reduces the load on the second or higher stage compressor(s), which improves process efficiency. Use of the heavy fraction in an independent pre-cool refrigeration loop can result in a near closure of the heating/cooling curves at the warm end of the heat exchanger, which results in more efficient refrigeration.
“Cold vapor” separation has been used to fractionate high pressure vapor into liquid and vapor streams. See, e.g., U.S. Pat. No. 6,334,334 to Stockmann et al., discussed above; “State of the Art LNG Technology in China”, Lange, M., 5th Asia LNG Summit, Oct. 14, 2010; “Cryogenic Mixed Refrigerant Processes”, International Cryogenics Monograph Series, Venkatarathnam, G., Springer, pp 199-205; and “Efficiency of Mid Scale LNG Processes Under Different Operating Conditions”, Bauer, H., Linde Engineering. In another process, marketed by Air Products as the AP-SMR™ LNG process, a “warm”, mixed refrigerant vapor is separated into cold mixed refrigerant liquid and vapor streams. See, e.g., “Innovations in Natural Gas Liquefaction Technology for Future LNG Plants and Floating LNG Facilities”, International Gas Union Research Conference 2011, Bukowski, J. et al. In these processes, the thus-separated cold liquid is used as the middle temperature refrigerant by itself and remains separate from the thus-separated cold vapor prior to joining a common return stream. The cold liquid and vapor streams, together with the rest of the returning refrigerants, are recombined via cascade and exit together from the bottom of the heat exchanger.
In the vapor separation systems discussed above, the warm temperature refrigeration used to partially condense the liquid in the cold vapor separator is produced by the liquid from the high-pressure accumulator. The present inventors have found that this requires higher pressure and less than ideal temperatures, both of which undesirably consume more power during operation.
Another process that uses cold vapor separation, albeit in a multi-stage, mixed refrigerant system, is described in GB Pat. No. 2,326,464 to Costain Oil. In this system, vapor from a separate reflux heat exchanger is partially condensed and separated into liquid and vapor streams. The thus-separated liquid and vapor streams are cooled and separately flashed before rejoining in a low-pressure return stream. Then, before exiting the main heat exchanger, the low-pressure return stream is combined with a subcooled and flashed liquid from the aforementioned reflux heat exchanger and then further combined with a subcooled and flashed liquid provided by a separation drum set between the compressor stages. In this system, the “cold vapor” separated liquid and the liquid from the aforementioned reflux heat exchanger are not combined prior to joining the low-pressure return stream. That is, they remain separate before independently joining up with the low-pressure return stream. As will be explained more fully below, the present inventors have found that power consumption can be significantly reduced by, inter alia, mixing a liquid obtained from a high-pressure accumulator with the cold vapor separated liquid prior to their joining a return stream.
Tables 1 and 2 show stream data for several embodiments of the invention and correlate with
There are several aspects of the present subject matter which may be embodied separately or together in the devices and systems described and claimed below. These aspects may be employed alone or in combination with other aspects of the subject matter described herein, and the description of these aspects together is not intended to preclude the use of these aspects separately or the claiming of such aspects separately or in different combinations as set forth in the claims appended hereto.
In one aspect, a system for cooling a feed fluid with a mixed refrigerant includes a main heat exchanger including a warm end and a cold end with a feed fluid cooling passage extending therebetween, the feed fluid cooling passage being configured to receive a feed fluid at the warm end and to convey a cooled feed fluid out of the cold end. The main heat exchanger also includes a high pressure vapor passage, a high pressure liquid passage, a cold separator vapor cooling passage, a cold separator liquid cooling passage and a primary refrigeration passage. A mixed refrigerant compressor system includes a compressor configured to receive a vapor phase or mixed phase refrigerant return stream from the primary refrigeration passage of the heat exchanger, an aftercooler configured to receive a compressed refrigerant stream from the compressor and a high pressure separation device having an inlet in fluid communication with the aftercooler outlet and a high pressure liquid outlet and a high pressure vapor outlet. The high pressure vapor cooling passage of the heat exchanger is configured to receive a high pressure vapor stream from the high pressure vapor outlet of the high pressure separation device and to cool the high pressure vapor stream to form a mixed phase stream. A cold vapor separator is configured to receive the mixed phase stream from the high pressure vapor cooling passage of the heat exchanger and has a cold separator liquid outlet and a cold separator vapor outlet. The cold separator vapor cooling passage of the heat exchanger is configured to receive and condense a cold separator vapor stream from the vapor outlet of the cold vapor separator so that a condensed cold separator stream is formed. A first expansion device is configured to receive and expand the condensed cold separator stream from the cold separator vapor cooling passage of the heat exchanger so that a cold temperature refrigerant stream is formed. The high pressure liquid cooling passage of the heat exchanger has a first heat exchange passage length and is configured to receive and subcool at least a portion of a mid-boiling refrigerant liquid stream from the high pressure liquid outlet of the high pressure separation device so that a subcooled mid-boiling refrigerant liquid stream is formed. The cold separator liquid cooling passage of the heat exchanger has a second heat exchange passage length, where the first heat exchange passage is separate and distinct from the second heat exchange passage and the first heat exchange passage length is greater than the second heat exchange passage length. The cold separator liquid cooling passage is configured to receive and subcool a cold separator liquid stream from the cold separator liquid outlet so that a subcooled cold separator liquid stream is formed. A junction is configured to combine the subcooled mid-boiling refrigerant liquid stream and the subcooled cold separator liquid stream while the subcooled mid-boiling refrigerant liquid stream is at, or colder via expansion than, the temperature of the subcooled mid-boiling refrigerant liquid stream in the subcooled state and the subcooled cold separator liquid stream is at, or colder via expansion than, the temperature of the subcooled cold separator liquid stream in the subcooled state so that a middle temperature refrigerant stream is formed. The primary refrigeration passage of the heat exchanger is configured to receive the cold temperature refrigerant stream from the first expansion device and the middle temperature stream from the junction and to thermally contact a feed fluid in the feed fluid cooling passage of the heat exchanger to form a cooled feed fluid in the feed fluid cooling passage and a vapor phase or mixed phase refrigerant return stream in the primary refrigeration passage.
A process flow diagram and schematic illustrating an embodiment of a multi-stream heat exchanger is provided in
As illustrated in
In one embodiment, referring to
It should be noted herein that the passages and streams are sometimes both referred to by the same element number set out in the figures. Also, as used herein, and as known in the art, a heat exchanger is that device or an area in the device wherein indirect heat exchange occurs between two or more streams at different temperatures, or between a stream and the environment. As used herein, the terms “communication”, “communicating”, and the like generally refer to fluid communication unless otherwise specified. And although two fluids in communication may exchange heat upon mixing, such an exchange would not be considered to be the same as heat exchange in a heat exchanger, although such an exchange can take place in a heat exchanger. A heat exchange system can include those items though not specifically described are generally known in the art to be part of a heat exchanger, such as expansion devices, flash valves, and the like. As used herein, the term “reducing the pressure of” does not involve a phase change, while the term, “flashing”, does involve a phase change, including even a partial phase change. As used herein, the terms, “high”, “middle”, “warm” and the like are relative to comparable streams, as is customary in the art. The stream tables 1 and 2 set out exemplary values as guidance, which are not intended to be limiting unless otherwise specified.
In an embodiment, the heat exchanger includes a high pressure vapor passage 166 adapted to receive a high pressure vapor stream 34 at the warm end and to cool the high pressure vapor stream 34 to form a mixed phase cold separator feed stream 164, and including an outlet in communication with a cold vapor separator VD4, the cold vapor separator VD4 adapted to separate the cold separator feed stream 164 into a cold separator vapor stream 160 and a cold separator liquid stream 156. In one embodiment, the high pressure vapor 34 is received from a high pressure accumulator separation device on the compression side.
In an embodiment, the heat exchanger includes a cold separator vapor passage having an inlet in communication with the cold vapor separator VD4. The cold separator vapor is cooled passage 168 condensed into liquid stream 112, and then flashed with 114 to form the cold temperature refrigerant stream 122. The cold temperature refrigerant 122 then enters the primary refrigeration passage at the cold end thereof. In one embodiment, the cold temperature refrigerant is a mixed phase.
In an embodiment, the cold separator liquid 156 is cooled in passage 157 to form subcooled cold vapor separator liquid 128. This stream can join the subcooled mid-boiling refrigerant liquid 124, discussed below, which, thus combined, are then flashed at 144 to form the middle temperature refrigerant 148, such as shown in
In an embodiment, the heat exchanger includes a high pressure liquid passage 136. In one embodiment, the high pressure liquid passage receives a high pressure liquid 38 from a high pressure accumulator separation device on the compression side. In one embodiment, the high pressure liquid 38 is a mid-boiling refrigerant liquid stream. The high pressure liquid stream enters the warm end and is cooled to form a subcooled refrigerant liquid stream 124. As noted above, the subcooled cold separator liquid stream 128 is combined with the subcooled refrigerant liquid stream 124 to form a middle temperature refrigerant stream 148. In an embodiment, the one or both refrigerant liquids 124 and 128 can independently be flashed at 126 and 130 before combining into the middle temperature refrigerant 148, as shown for example in
In an embodiment, the cold temperature refrigerant 122 and middle temperature refrigerant 148, thus combined, provide refrigeration in the primary refrigeration passage 104, where they exit as a vapor phase or mixed phase refrigerant return stream 104A/102. In an embodiment, they exit as a vapor phase refrigerant return stream 104A/102. In one embodiment, the vapor is a superheated vapor refrigerant return stream.
As shown in
In an embodiment, the warm temperature refrigerant stream 158 enters the pre-cool refrigerant passage 108 to provide cooling. In an embodiment, the pre-cool refrigerant passage 108 provides substantial cooling for the high pressure vapor passage 166, for example, to cool and condense the high pressure vapor 34 into the mixed phase cold separator feed stream 164.
In an embodiment, the warm temperature refrigerant stream exits the pre-cool refrigeration passage 108 as a vapor phase or mixed phase warm temperature refrigerant return stream 108A. In an embodiment, the warm temperature refrigerant return stream 108A returns to the compression side either alone—such as shown in
In an embodiment, the warm temperature refrigerant stream 158, rather than entering the pre-cool refrigerant passage 108, instead is introduced to the primary refrigerant passage 204, such as shown in
Referring to
Vapor stream 24 is provided to the compressor 26 via an inlet in communication with the interstage separation device VD2, which compresses the vapor 24 to provide compressed fluid stream 28. An optional aftercooler 30 if present cools the compressed fluid stream 28 to provide an a high pressure mixed phase stream 32 to the accumulator separation device VD3. The accumulator separation device VD3 separates the high pressure mixed phase stream 32 into high pressure vapor stream 34 and a high pressure liquid stream 36, which may be a mid-boiling refrigerant liquid stream. In an embodiment, the high pressure vapor stream 34 is sent to the high pressure vapor passage of the heat exchanger.
An optional splitting intersection is shown, which has an inlet for receiving the mid-high pressure liquid stream 36 from the accumulator separation device VD3, an outlet for providing a mid-boiling refrigerant liquid stream 38 to the heat exchanger, and optionally an outlet for providing a fluid stream 40 back to the interstage separation device VD2. An optional expansion device 42 for stream 40 is shown which, if present provides a an expanded cooled fluid stream 44 to the interstage separation device, the interstage separation device VD2 optionally further comprising an inlet for receiving the fluid stream 44. If the splitting intersection is not present, then the mid-boiling refrigerant liquid stream 36 is in direct fluid communication with mid-boiling refrigerant liquid stream 38.
Furthermore, while the present system and method are described below in terms of liquefaction of natural gas, they may be used for the cooling, liquefaction and/or processing of gases other than natural gas including, but not limited to, air or nitrogen.
The removal of heat is accomplished in the heat exchanger using a single mixed refrigerant in the systems described herein. Exemplary refrigerant compositions, conditions and flows of the streams of the refrigeration portion of the system, as described below, which are not intended to be limiting, are presented in Tables 1 and 2.
In one embodiment, warm, high pressure, vapor refrigerant stream 34 is cooled, condensed and subcooled as it travels through high pressure vapor passage 166/168 of the heat exchanger 170. As a result, stream 112 exits the cold end of the heat exchanger 170. Stream 112 is flashed through expansion valve 114 and re-enters the heat exchanger as stream 122 to provide refrigeration as stream 104 traveling through primary refrigeration passage 104. As an alternative to the expansion valve 114, another type of expansion device could be used, including, but not limited to, a turbine or an orifice.
Warm, high pressure liquid refrigerant stream 38 enters the heat exchanger 170 and is subcooled in high pressure liquid passage 136. The resulting stream 124 exits the heat exchanger and is flashed through expansion valve 126. As an alternative to the expansion valve 126, another type of expansion device could be used, including, but not limited to, a turbine or an orifice. Significantly, the resulting stream 132 rather than re-entering the heat exchanger 170 directly to join the primary refrigeration passage 104, first joins the subcooled cold separator vapor liquid 128 to form a middle temperature refrigerant stream 148. The middle temperature refrigerant stream 148 then re-enters the heat exchanger wherein it joins the low pressure mixed phase stream 122 in primary refrigeration passage 104. Thus combined, and warmed, the refrigerants exit the warm end of the heat exchanger 170 as vapor refrigerant return stream 104A, which may be optionally superheated.
In one embodiment, vapor refrigerant return stream 104A and stream 108A which, may be mixed phase or vapor phase, may exit the warm end of the heat exchanger separately, e.g., each through a distinct outlet, or they may be combined within the heat exchanger and exit together, or they may exit the heat exchanger into a common header attached to the heat exchanger before returning to the suction separation device VD1. Alternatively, streams 104A and 108A may exit separately and remain so until combining in the suction separation device VD1, or they may, through vapor and mixed phase inlets, respectively, and are combined and equilibrated in the low pressure suction drum. While a suction drum VD1 is illustrated, alternative separation devices may be used, including, but not limited to, another type of vessel, a cyclonic separator, a distillation unit, a coalescing separator or mesh or vane type mist eliminator. As a result, a low pressure vapor refrigerant stream 14 exits the vapor outlet of drum VD1. As stated above, the stream 14 travels to the inlet of the first stage compressor 16. The blending of mixed phase stream 108A with stream 104A, which includes a vapor of greatly different composition, in the suction drum VD1 at the suction inlet of the compressor 16 creates a partial flash cooling effect that lowers the temperature of the vapor stream traveling to the compressor, and thus the compressor itself, and thus reduces the power required to operate it.
In one embodiment, a pre-cool refrigerant loop enters the warm side of the heat exchanger 170 and exits with a significant liquid fraction. The partially liquid stream 108A is combined with spent refrigerant vapor from stream 104A for equilibration and separation in suction drum VD1, compression of the resultant vapor in compressor 16 and pumping of the resulting liquid by pump P. In the present case, equilibrium is achieved as soon as mixing occurs, i.e., in the header, static mixer, or the like. In one embodiment, the drum merely protects the compressor. The equilibrium in suction drum VD1 reduces the temperature of the stream entering the compressor 16, by both heat and mass transfer, thus reducing the power usage by the compressor.
Other embodiments shown in
In one embodiment, the warm temperature refrigerant passage 158 is in fluid communication with an accumulator separation device VD5 having a vapor outlet in fluid communication with a warm temperature refrigerant vapor passage 158v and a liquid outlet in fluid communication with a warm temperature refrigerant liquid passage 158l.
In one embodiment, the warm temperature refrigerant vapor and liquid passages 158v and 158l are in fluid communication with the low pressure high-boiling stream passage 108.
In one embodiment, the warm temperature refrigerant vapor and liquid passages 158v and 158l are in fluid communication with each other either inside the heat exchanger or in a header outside the heat exchanger.
In one embodiment, the flashed cold separator liquid stream passage 134 is in fluid communication with an accumulator separation device VD6 having a vapor outlet in fluid communication with a middle temperature refrigerant vapor passage 148v, and a liquid outlet in fluid communication with a middle temperature refrigerant liquid passage 148l.
In one embodiment, the middle temperature refrigerant vapor and liquid passages 148v and 148l are in fluid communication with the low pressure mixed refrigerant passage 104.
In one embodiment, the middle temperature refrigerant vapor and liquid passages 148v and 148l are in fluid communication with each other either inside the heat exchanger or in a header outside the heat exchanger.
In one embodiment, the flashed mid-boiling refrigerant liquid stream passage 132 is in fluid communication with an accumulator separation device VD6 having a vapor outlet in fluid communication with a middle temperature refrigerant vapor passage 148v and a liquid outlet in fluid communication with a middle temperature refrigerant liquid passage 148l.
In one embodiment, the middle temperature refrigerant vapor and liquid passages 148v and 148l are in fluid communication with the low pressure mixed refrigerant passage 104.
In one embodiment, the middle temperature refrigerant vapor and liquid passages 148v and 148l are in fluid communication with each other either inside the heat exchanger or in a header outside the heat exchanger.
In one embodiment, the flashed mid-boiling refrigerant liquid stream 132 and the flashed cold separator liquid stream 134 are in fluid communication with an accumulator separation device VD6 having a vapor outlet in fluid communication with a middle temperature refrigerant vapor passage 148v and a liquid outlet in fluid communication with a middle temperature refrigerant liquid passage 148l.
In one embodiment, the middle temperature refrigerant vapor and liquid passages 148v and 148l are in fluid communication with the low pressure mixed refrigerant passage 104.
In one embodiment, the middle temperature refrigerant vapor and liquid passages 148v and 148l are in fluid communication with each other either inside the heat exchanger or in a header outside the heat exchanger.
In one embodiment, the flashed mid-boiling refrigerant liquid stream 132 and the flashed cold separator liquid stream 134 are in fluid communication with each other prior to fluidly communicating with the accumulator separation device VD6.
In one embodiment, the low pressure mixed phase stream passage 122 is in fluid communication with an accumulator separation device VD7 having a vapor outlet in fluid communication with a cold temperature refrigerant vapor passage 122v, and a cold temperature liquid passage 122l.
In one embodiment, the cold temperature refrigerant vapor passage 122v and a cold temperature liquid passage 122l are in fluid communication with the low pressure mixed refrigerant passage 104.
In one embodiment, the cold temperature refrigerant vapor passage 122v and cold temperature liquid passage 122l are in fluid communication with each other either inside the heat exchanger or in a header outside the heat exchanger.
In one embodiment, each of the warm temperature refrigerant passage 158, flashed cold separator liquid stream passage 134, low pressure mid-boiling refrigerant passage 132, low pressure mixed phase stream passage 122 is in fluid communication with a separation device.
In one embodiment, one or more precooler may be present in series between elements 16 and VD2.
In one embodiment, one or more precooler may be present in series between elements 30 and VD3.
In one embodiment, a pump may be present between a liquid outlet of VD1 and the inlet of VD2. In some embodiments, a pump may be present between a liquid outlet of VD1 and having an outlet in fluid communication with elements 18 or 22.
In one embodiment, the pre-cooler is a propane, ammonia, propylene, ethane, pre-cooler.
In one embodiment, the pre-cooler features 1, 2, 3, or 4 multiple stages.
In one embodiment, the mixed refrigerant comprises 2, 3, 4, or 5 C1-C5 hydrocarbons and optionally N2.
In one embodiment, the suction separation device includes a liquid outlet and further comprising a pump having an inlet and an outlet, wherein the outlet of the suction separation device is in fluid communication with the inlet of the pump, and the outlet of the pump is in fluid communication with the outlet of the aftercooler.
In one embodiment, the mixed refrigerant system a further comprising a pre-cooler in series between the outlet of the intercooler and the inlet of the interstage separation device and wherein the outlet of the pump is also in fluid communication with the pre-cooler.
In one embodiment, the suction separation device is a heavy component refrigerant accumulator whereby vaporized refrigerant traveling to the inlet of the compressor is maintained generally at a dew point.
In one embodiment, the high pressure accumulator is a drum.
In one embodiment, an interstage drum is not present between the suction separation device and the accumulator separation device.
In one embodiment, the first and second expansion devices are the only expansion devices in closed-loop communication with the main process heat exchanger.
In one embodiment, an aftercooler is the only aftercooler present between the suction separation device and the accumulator separation device.
In one embodiment, the heat exchanger does not have a separate outlet for a pre-cool refrigeration passage.
In an alternative embodiment, described below with reference to
A conventional cascade refrigeration layout for acid gas distillation units has several issues, including high operating power and a high equipment count. The latter leads to higher capital expenditures and a larger plot space requirement. When applying the technology of the disclosure as a refrigeration system for an acid gas distillation unit, the refrigeration equipment count is significantly reduced. The multiple pure component refrigeration loops with multiple compression stages associated with a cascade refrigeration layout are replaced with a single mixed refrigerant loop with preferably a two-stage compressor. The use of a mixed refrigerant system and associated brazed aluminum heat exchangers (BAHX) also allows for additional process heating and cooling loads from the acid gas distillation unit to be integrated with the refrigeration system. This results in a further reduction in the total equipment count, and the required refrigeration flow/duty. This provides a significant reduction in operating power, and a reduction in the size of the refrigerant compressor and associated equipment.
An example of a cryogenic acid gas distillation system and process suitable for use with the technology of the disclosure is described in U.S. Pat. No. 9,945,605 to Pellegrini, issued Apr. 17, 2018, the contents of which is hereby incorporated by reference. The system and process disclosed by the Pellegrini '605 patent requires an external refrigeration source to generate the reflux for one or more distillation columns. This external refrigeration requirement can be met with a single mixed refrigerant system, such as the system indicated in general at 310 in
The mixed refrigerant system of
With continued reference to
The cold vapor separator vapor stream 342 is condensed and subcooled in passage 346 and then is flashed across an expansion device 352, such as a Joules Thomson (T) valve. The resulting mixed phase refrigerant stream is directed to primary refrigeration passage 354.
The liquid stream 344 from the cold vapor separator is subcooled in the cold separator liquid cooling passage, while the liquid stream 326 from the high pressure accumulator 322 is subcooled in a high pressure liquid passage 358. The resulting subcooled streams can independently be flashed via expansion devices at 362 and 364 before combining into the middle temperature refrigerant stream 366, which is directed to the primary refrigeration passage 354.
The streams from passages 346, 348 and 358 exit the heat exchanger at appropriate locations based on the optimized amount of subcooling for each stream. The flashed mixed refrigerant streams are then fed back to the heat exchanger at the appropriate locations based on the stream temperatures. The flashing provides the temperature driving force/duty required for the acid gas distillation process cooling loads as well as the aforementioned cooling of fluid flowing in passages 346, 348 and 358.
The use of a BAHX/Cold Box system allows for multiple process side heating and cooling loads, and mixed refrigerant heating and cooling loads to be integrated into a single heat exchanger service. This helps to minimize the refrigeration load as multiple variables of the mixed refrigerant system (suction pressure, mixed refrigerant composition, subcooling temperatures, etc.) can be adjusted to provide cooling at the exact temperature ranges required. Additionally, the high surface area to volume ratio of BAHX allows for a low mean temperature differential and minimum internal temperature approaches resulting in lower refrigerant flow/duty requirements.
The net result is a compact refrigeration system, with a low refrigeration equipment count and equipment sizes relative to the process capacity. The number of exchanger services and expansion device locations, etc. of
The contents of U.S. Pat. No. 10,345,039 to Gushanas et al., issued Jul. 9, 2019; U.S. Pat. No. 9,441,877 to Gushanas et al., issued Sep. 13, 2016; U.S. Pat. No. 6,333,445 to O'Brien, issued Dec. 25, 2001, and U.S. Pat. No. 9,945,605 to Pellegrini, issued Apr. 17, 2018, are hereby incorporated by reference.
While 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 may be made therein without departing from the spirit of the invention, the scope of which is defined by the claims and elsewhere herein.
This application is a continuation-in-part of U.S. patent application Ser. No. 16/545,695, filed Aug. 20, 2019, which is a continuation-in-part of U.S. patent application Ser. No. 14/218,949, filed Mar. 18, 2014, which claims priority to U.S. Provisional Patent Application No. 61/802,350, filed Mar. 15, 2013, the entire contents of each of which are hereby incorporated by reference.
| Number | Date | Country | |
|---|---|---|---|
| 61802350 | Mar 2013 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 16545695 | Aug 2019 | US |
| Child | 16856555 | US | |
| Parent | 14218949 | Mar 2014 | US |
| Child | 16545695 | US |
