Patent Grant
10371441
The present application is a National Stage (§ 371) application of PCT/EP2015/065692, filed Jul. 9, 2015, which claims the benefit of European Application No. 14178262.3, filed Jul. 24, 2014, which is incorporated herein by reference in its entirety.
The present invention relates to a hydrocarbon condensate stabilizer, and a method of producing a stabilized hydrocarbon condensate stream.
A condensate stabilizing process is disclosed in US pre-grant publication number 2009/0188279, wherein a debutanizer/stabilizer column is employed. The stabilizer column discharges a vaporous stream being enriched in butane and lower hydrocarbons (such as methane, ethane and/or propane) relative to a liquid stream being discharged from the bottom of the stabilizer column. The vaporous stream is cooled against an ambient stream in an air cooler or water cooler, and fed to an overhead condenser drum. The liquid bottom stream removed at an outlet from the overhead condenser drum is pressurized in a pump and returned as a reflux stream to the top of the stabilizer column. The remaining vapour is also removed from the overhead condenser drum and subsequently combined with another vaporous stream obtained from a gas/liquid separator. The combined vapour streams are compressed thereby obtaining a product gas which may be subjected to a liquefaction stream in one or more heat exchangers thereby obtaining liquefied natural gas (LNG).
The stabilizer column is fed by a liquid bottom stream from the gas/liquid separator. This liquid bottom stream is an unstabilized hydrocarbon condensate stream as in addition to C5+ (pentanes and higher hydrocarbon components) the liquid bottom stream also may contain lighter hydrocarbons (particularly propane and/or butane). This unstabilized hydrocarbon condensate stream is indirectly heat exchanged against a major part of the liquid stream (condensate) being discharged from the bottom of the stabilizer column.
As a result of varying composition of the unstabilized hydrocarbon condensate stream, the dew point of the stabilizer column overhead vapour may vary over a wide temperature range between the multiple feed cases. With the condensate stabilizing process as disclosed in US 2009/0188279 described above, an air or water cooled condenser does not result in sufficient condensation in all these cases since the dew point of the vapour is typically close or below the ambient cooling medium supply temperatures. In other instances there may be an excess of condensation leading to too much reflux. Hence, the condensate stabilizing process as disclosed in US 2009/0188279 has the problem that a continuous top feed/reflux cannot be guaranteed in all cases.
In accordance with a first aspect of the present invention, there is provided a method of producing a stabilized hydrocarbon condensate stream, comprising:
In accordance with another aspect of the invention, there is provided a hydrocarbon condensate stabilizer for producing a stabilized hydrocarbon condensate, comprising:
The invention will be further illustrated hereinafter by way of example only, and with reference to the non-limiting drawing in which;
For the purpose of this description, a single reference number will be assigned to a line as well as a stream carried in that line. Same reference numbers refer to similar components. The person skilled in the art will readily understand that, while the invention is illustrated making reference to one or more a specific combinations of features and measures, many of those features and measures are functionally independent from other features and measures such that they can be equally or similarly applied independently in other embodiments or combinations.
A mixed phase pressurized unstabilized hydrocarbon stream is fed into a stabilizer column at a feed pressure. A liquid phase of stabilized hydrocarbon condensate is discharged from a bottom end of the stabilizer column, while a vapour phase of volatile components from the pressurized unstabilized hydrocarbon condensate stream is discharged from a top end of the stabilizer column. The vapour phase being discharged from the top end of the stabilizer column is compressed and subsequently passed through an overhead condenser wherein partial condensation takes place by indirect heat exchange against a coolant. The overhead condenser is provided in the form of an ambient heat exchanger, in which case an ambient stream (air or water) is used as the coolant. The resulting partially condensed overhead stream is separated in an overhead separator into a vapour effluent stream and an overhead liquid stream. After discharging the overhead liquid stream from the overhead separator, it is selectively divided into a liquid reflux stream and a liquid effluent stream. The liquid reflux stream is expanded to the feed pressure and fed into the stabilizer column.
One of the modifications compared to the prior art that is currently proposed is to compress the vapour phase being discharged from the top end of the stabilizer column thereby forming a compressed overhead vapour stream prior to passing through an ambient heat exchanger wherein partially condensing the compressed overhead vapour stream. As a result of the increased pressure of the compressed overhead vapour stream relative to the vapour phase being discharged from the top end of the stabilizer, the dew point temperature of the vapour increases and may be notably above the supply temperature of the typical ambient cooling medium. Thus, condensation occurs for all the feed cases when the stream is cooled and condensed using cooling against an ambient stream, which can be ambient air and/or ambient water.
Another of the proposed modifications compared to the prior art is selectively dividing the overhead liquid stream being discharged from the overhead separator into a liquid reflux stream and a liquid effluent stream. This facilitates to discharge excess liquids that may form upon the condensing of the vapour phase being discharged from the top end of the stabilizer, which may particularly happen as a result of the previous discussed modification whereby the condensation takes place at higher pressure. Hence, this second modification mitigates against undesired excess condensation.
Suitably, the pressurized unstabilized hydrocarbon condensate stream is partially evaporated in a feed-effluent heat exchanger to form a mixed phase pressurized unstabilized hydrocarbon stream out of the pressurized unstabilized hydrocarbon condensate stream prior to being fed to the stabilizer column. The vapour effluent stream from the overhead separator or the effluent liquid stream discussed above, or both, may be supplied to the feed-effluent heat exchanger to supply the heat required to partially evaporate the pressurized unstabilized hydrocarbon condensate stream. Since the vapour effluent stream and/or the effluent liquid stream have been formed by indirect heat exchanging against an ambient stream, the temperature of the vapour effluent stream and/or the effluent liquid stream is well suited to produce the mixed phase pressurized unstabilized hydrocarbon stream at a temperature that is suited for feeding into the stabilizer column at a relatively high level, above a first vapour/liquid contacting device.
Moreover, by using heat from the vapour effluent stream and/or the effluent liquid stream to partially vaporize the pressurized unstabilized hydrocarbon condensate stream, the vapour effluent stream and/or the effluent liquid stream are cooled. This is particularly beneficial if the effluent stream(s) are intended to be subject to further refrigeration as this would save on cooling duty required in the further refrigeration. Further refrigeration may suitably be done by reinjecting the effluent stream(s) in a lean natural gas stream which has passed through a liquids extraction device, whereby the liquids extraction device has served to extract the pressurized unstabilized hydrocarbon condensate stream from a natural gas stream to produce the lean natural gas stream.
Turning now to
The natural gas liquefaction train 100 is intended to implement a natural gas liquefaction process. Many such natural gas liquefaction processes are known and understood by the person skilled in the art, and need not be fully described in the present application. For the present application, a few elements or parts of the natural gas liquefaction train 100 are highlighted.
The natural gas liquefaction train 100 typically comprises one or more pre-cooling heat exchangers 110 wherein a pressurized natural gas feed stream 10 can be refrigerated. Alternatively, an expander is used to extract enthalpy from the pressurized natural gas feed stream 10. This will be further illustrated later herein, with reference to
The pressure of the pressurized natural gas feed stream 10 may be in the range of from 40 bara to 80 bara. The pressurized natural gas feed stream may comprise methane (“C1”), ethane (“C2”), propane (“C3”), butanes (“C4” consisting of n-butane and i-butane), and pentanes and higher hydrocarbon components (“C5+”). Higher hydrocarbon components possibly include aromatics. Although this is not always the case, the pressurized natural gas feed stream may comprise one or more volatile inert components, of which typically mainly nitrogen, in addition to the other components. Volatile inert components are nitrogen, argon, and helium. These are inert components that are more volatile than methane.
The pressurized natural gas feed stream 10 may find its origin from a hydrocarbon obtained from natural gas or petroleum reservoirs or coal beds, or from another source, including as an example a synthetic source such as a Fischer-Tropsch process, or from a mix of different sources. Initially the hydrocarbon stream may comprise at least 50 mol % methane, more preferably at least 80 mol % methane.
Depending on their source, one or more of the hydrocarbon streams may contain varying amounts of components other than methane and volatile inert components, including one or more non-hydrocarbon components, such as water, CO2, Hg, H2S and other sulphur compounds; and one or more hydrocarbons heavier than methane such as in particular ethane, propane and butanes, and, possibly lesser amounts of pentanes and aromatic hydrocarbons.
In those cases, the hydrocarbon streams may have been dried and/or pre-treated to reduce and/or remove one or more of undesired components such as CO2, Hg, and water. Furthermore, the hydrocarbon streams may have undergone other steps such as pre-pressurizing or the like. Such steps are well known to the person skilled in the art, and their mechanisms are not further discussed here. The pressurized natural gas feed stream 10 is assumed to be the result of any selection of such steps as needed. The ultimate composition of the pressurized natural gas feed stream 10 thus varies depending upon the type and location of the gas and the applied pre-treatment(s).
Referring again to
The liquids extraction device 120 can be any suitable type of extraction device, ranging from a fully refluxed and reboiled natural gas liquids extraction column to a simple separation vessel, or separation drum, based on only one theoretical separation stage. In between those extremes is a scrub column. Such liquids extraction device 120 is normally operated below the critical point of the pressurized natural gas feed stream 10. However, a simple separation vessel, or separation drum, based on only one theoretical separation stage may be operated in the retrograde region within the phase envelope of the pressurized natural gas feed stream 10.
A lean natural gas stream may be discharged from the liquids extraction device 120 simultaneously with the pressurized unstabilized hydrocarbon condensate stream 210. The term “lean” in the present context means that the relative amounts of C5+ in the lean natural gas stream are lower than in the pressurized natural gas feed stream 10. In the embodiment of
The natural gas liquefaction train 100 typically further comprises a further refrigerator 130, wherein the lean pressurized refrigerated natural gas stream 30 may be further refrigerated. As further refrigeration typically is performed to fully condense the lean pressurized refrigerated natural gas stream 30, the lean pressurized refrigerated natural gas stream 30 normally meets a maximum specification of solidifying components, including water, CO2 and C5+. Such maximum specification is governed by the need to avoid solidification. However, some operators or plant owners voluntarily choose to maintain an additional margin. In one example, the maximum specification for water may typically be less than 1 ppmv, for CO2 less than 50 ppmv, and for C5+ less than 0.1 mol %.
In the example of
Referring still to
In such end flash unit, the fully condensed lean pressurized refrigerated natural gas stream 40 being discharged from the further refrigerator 130 is subsequently depressurized to a pressure of for instance less than 2 bara, whereby producing a flash vapour stream 70 and a liquefied natural gas stream 60. The flash vapour stream 70 and the liquefied natural gas stream 60 may be separated from each other in the end-flash separator 150. The liquefied natural gas stream 60 is typically passed to a storage tank 160. With such end flash unit, it is possible to pass the lean pressurized refrigerated natural gas stream 30 through the further refrigerator 130 in pressurized condition, for instance at a pressure of between 40 and 80 bar absolute, or between 50 and 70 bar absolute, while storing any liquefied part of the fully condensed lean pressurized refrigerated natural gas stream 40 at substantially atmospheric pressure, such as between 1 and 2 bar absolute.
Depending on the separation requirements, governed for instance by the amount of volatile inert components in the lean pressurized refrigerated natural gas stream 30, the end flash separator may be provided in the form of a simple drum which separates vapour from liquid phases in a single equilibrium stage, or a more sophisticated vessel such as a distillation column. Non-limiting examples of possibilities are disclosed in U.S. Pat. Nos. 5,421,165; 5,893,274; 6,014,869; 6,105,391; and pre-grant publication US 2008/0066492. In some of these examples, the more sophisticated vessel is connected to a reboiler whereby the fully condensed lean pressurized refrigerated natural gas stream 40, before being expanded in said pressure reduction system, is led to pass though a reboiler in indirect heat exchanging contact with a reboil stream from the vessel, whereby the fully condensed lean pressurized refrigerated natural gas stream 40 is caused to give off heat to the reboil stream.
The compressor cooler 105 in the embodiment of
Similar to
The remaining parts in
Referring again to
The pressurized unstabilized hydrocarbon condensate stream 210 is provided through a pressure line 210. In
The stabilizer column 400 comprises a bottom end 460 that is located gravitationally lower than the first inlet device 410. Suitably, the bottom end 460 is separated from the first inlet device 410 by a first vapour/liquid contacting device 470. Furthermore, the stabilizer column 400 comprises a second inlet device 420 at a level gravitationally above the first inlet device 410, wherein the first inlet device 410 and the second inlet device 420 are separated from each other by a second vapour/liquid contacting device 450. The stabilizer column 400 further comprises a top end 440, which top end 440 is located in the stabilizer column 400 gravitationally higher than the second inlet device 420. A liquid discharge line 250 is fluidly connected to the bottom end 460 of the stabilizer column 400, and arranged to receive a liquid phase comprising stabilized hydrocarbon condensate that is discharged from the bottom end 460 of the stabilizer column 400. A vapour discharge line 270 is fluidly connected to the top end 440 of the stabilizer column 400, and arranged to receive a vapour phase comprising volatile components from the pressurized unstabilized hydrocarbon condensate stream 210 that is discharged from the top end 440 of the stabilizer column 400.
The first vapour/liquid contacting device 470 and/or the second vapour/liquid contacting device 450 may be embodied in any suitable form. They may be based on a number of contact trays, or on packing. Contact trays are available in a number of common variants, including sieve trays, valve trays, and bubble cap trays. Packing has at least two common variants: structured packing and random packing. A slight preference exists for structured packing.
The expansion device 375 may be provided in the form of a simple Joule-Thomson valve or it may have higher complexity. Regardless of the specific implementation of the expansion device 375, its function is to allow feeding of the mixed phase pressurized unstabilized hydrocarbon stream 240 at said feed pressure into the stabilizer column 400.
In the example shown in
An overhead compressor system 320 is arranged in the vapour discharge line 270, for compressing the vapour phase being discharged from the top end 440 of the stabilizer column 400 to an auxiliary pressure, thereby forming a compressed overhead vapour stream 280. The auxiliary pressure is higher than the feed pressure. An overhead line 280 is connected to the vapour discharge line 270 via the compressor system 320. The overhead compressor system 320 may further be provided with one or more compressor suction drums (not shown) to protect any overhead compressor in the overhead compressor system 320 against possible liquids that might be present in the vapour discharge line 270.
In the embodiment of
The overhead compressor system 320 may further comprise a de-superheater. In the embodiment as illustrated in
At the end of the overhead compressor system 320, all of the compressed overhead vapour part streams are recombined in a recombiner 325, which discharges into the overhead line 280.
Regardless of the specific lay out of the overhead compressor system 320, an ambient heat exchanger 340 is arranged in the overhead line 280. This ambient heat exchanger 340 is arranged to receive the compressed overhead vapour stream and bring the compressed overhead vapour stream in indirect heat exchanging contact with an ambient stream, whereby passing heat from the compressed overhead vapour stream to the ambient stream. As a result the compressed overhead vapour stream is partially condensed, whereby the compressed overhead vapour stream becomes a partially condensed overhead stream at the second temperature.
An overhead separator 350 is arranged in the overhead line 280 downstream of the ambient heat exchanger 340 and in fluid communication therewith. This overhead separator 350 is configured to receive the partially condensed overhead stream from the ambient heat exchanger 340, and to separate the partially condensed overhead stream into a vapour effluent stream and an overhead liquid stream. An effluent vapour line 290 is arranged to receive the vapour effluent stream being discharged from the overhead separator 350, and an overhead liquid line 390 is arranged to receive the overhead liquid stream being discharged from the overhead separator 350.
A stream splitter 380 is arranged in the overhead liquid line 390, for selectively dividing the overhead liquid stream being discharged from the overhead separator 350 at the second temperature into a liquid reflux stream and an effluent liquid stream. A liquid reflux line 415 is fluidly connected to the stream splitter 380, and arranged to receive the liquid reflux stream. The liquid reflux line 415 serves to convey the liquid reflux stream to the second inlet device 420 into the stabilizer column 400. A reflux expander 418 may be configured in the liquid reflux line 415 between the stream splitter 380 and the second inlet device 420 to adopt the pressure of the liquid reflux stream to the feed pressure. The reflux expander 418 also serves to regulate the flow rate of the liquid reflux stream in the liquid reflux line 415. An effluent liquid line 215 is also fluidly connected to the stream splitter 380. The effluent liquid line 215 is arranged to receive the effluent liquid stream.
The evaporator 310 may be any type of heat exchanger capable of adding heat to the pressurized unstabilized hydrocarbon condensate stream 210. In advantageous embodiments, the evaporator 310 is provided in the form of a feed-effluent heat exchanger as illustrated in
A flow regulating valve 218 may be configured in the effluent liquid line 215 between the overhead separator 350 and the feed-effluent heat exchanger. This flow regulating valve 218 is suitably liquid level controlled to keep a level of liquid resident in the overhead separator 350 within two acceptable predetermined limits. A pressure controlled valve 298 may be configured in the effluent vapour line 290 between the overhead separator 350 and the feed-effluent heat exchanger. Herewith the pressure in the overhead separator 350 can be kept constant.
Preferably, the stabilizer column 400 is a reboiled stabilizer column, whereby a heat source 490 is arranged to add heat to the bottom end 460 of the stabilizer column 400 below the first vapour/liquid contacting device 470. The heat source 490, commonly referred to as reboiler, is connected to a liquid draw off device 495 (such as a chimney plate) configured in the stabilizer column 400 and discharges heated liquid back into the bottom end 460 of the stabilizer column 400. Heat may be provided by indirect heat exchange against for instance hot oil.
A condensate cooler 455 may be configured in the liquid discharge line 250, to cool the liquid phase being discharged from the bottom end 460 of the stabilizer column 400 and thus create a cooled stream comprising the stabilized hydrocarbon condensate. A condensate splitter 454 may optionally be arrange in the liquid discharge line 250 downstream of the condensate cooler 455. This condensate splitter 454 serves to split the cooled stream comprising the stabilized hydrocarbon condensate into a recycle stream and a discharge stream. The condensate splitter 454 is fluidly connected to a condensate storage tank 265, optionally via a condensate flow valve 255, to convey the discharge stream to the condensate storage tank 265. The condensate splitter 454 is also connected to a condensate recycle line 451 to route the recycle stream back to the stabilizer column 400 at a level above the first vapour/liquid contacting device 470 and below the first inlet device 410. The third inlet device 430 can be used for this purpose. Suitably, the condensate recycle line 451 connects to the stabilizer column 400 via the liquid hydrocarbon feed line 251. Alternatively, the condensate recycle line 451 directly connects to the the third inlet device 430. A pump 457 is suitably configured in the condensate recycle line 451. Optionally, a recycle flow control valve 458 is configured in the condensate recycle line 451 as well, to control the recycle flow rate. Suitably, the recycle flow control valve 451 is configured at the high-pressure discharge side of the pump 457 to avoid cavitation.
In operation, the system of
The pressurized natural gas feed stream 10 is refrigerated, for instance in the one or more pre-cooling heat exchangers 110 as in the example of
The pressurized unstabilized hydrocarbon condensate stream 210 comprises at least the condensed C5+ components, and one or more of C1 to C4 components. The amount of methane and any volatile inert components in the pressurized unstabilized hydrocarbon condensate stream 210 may be in the range of from 50 mol % to 80 mol %, preferably in the range of from 60 mol % to 80 mol % of the pressurized unstabilized hydrocarbon condensate stream 210. Not all of the volatile inert components need to be present. The amount of volatile inert components in the pressurized unstabilized hydrocarbon condensate stream less than 10 mol %, preferably less than 2 mol %, of the pressurized unstabilized hydrocarbon condensate stream. Practically all of the methane and any volatile inert components will leave the stabilizer column 400 via the vapour discharge line 270, causing a relatively low dew point of the vapour phase in the vapour discharge line 270.
The pressurized unstabilized hydrocarbon condensate stream 210 is discharged from the liquids extraction device 120 at a first temperature. The first temperature is preferably below the ambient temperature. For example, the first temperature may be in a first temperature range of from −80° C. to −30° C. Preferably the upper limit of the first temperature range is −40° C. Preferably, the lower limit of the first temperature range is −70° C. The pressure may be close to the pressure of the pressurized natural gas feed stream 10, in the range of from 40 bara to 80 bara, or a few bar (between 2 and 10 bar) below the pressure of the pressurized natural gas feed stream 10, or significantly below the pressure of the pressurized natural gas feed stream 10 (by between 10 bar and 50 bar). In one example, the pressure was 59 bara, close to the pressure of the pressurized natural gas feed stream 10.
Simultaneously with the pressurized unstabilized hydrocarbon condensate stream 210, a lean natural gas stream is also discharged from the liquids extraction device 120. In the embodiment of
In either embodiment, the lean pressurized refrigerated natural gas stream 30 is then further refrigerated in the further refrigerator 130, whereby fully condensing the lean pressurized refrigerated natural gas stream. Subsequently, the lean pressurized refrigerated natural gas stream is depressurized, whereby producing a flash vapour stream and a liquefied natural gas stream. The pressure after the depressurizing is typically between 1 and 2 bara. The temperature of the liquefied natural gas stream is below −155° C., and usually below −160° C. The temperature of the liquefied natural gas stream may typically be −162° C.
The pressurized unstabilized hydrocarbon condensate stream 210 is then partially evaporated, whereby the pressurized unstabilized hydrocarbon condensate stream becomes a mixed phase pressurized unstabilized hydrocarbon stream 240 at an initial pressure. The mixed phase pressurized unstabilized hydrocarbon stream 240 is then expanded from said initial pressure to a feed pressure, and fed at the feed pressure into the stabilizer column 400 via the first inlet device 410. The feed pressure may be in a feed pressure range of from 2 bara to 25 bara, preferably in a feed pressure range of from 2 bara to 20 bara. Preferably, the lower limit of these ranges is 5 bara. In one example, the feed pressure was 12 bara.
The expanding of the mixed phase pressurized unstabilized hydrocarbon stream 240 from the initial pressure to the feed pressure and the feeding of the mixed phase pressurized unstabilized hydrocarbon stream 240 into the stabilizer column 400 may be done in a variety of ways. In the example of
Optionally, and as illustrated in
A liquid phase comprising stabilized hydrocarbon condensate is discharged from the bottom end 460 of the stabilizer column 400. A vapour phase comprising volatile components from the pressurized unstabilized hydrocarbon condensate stream 210 is discharged from the top end 440 of the stabilizer column 400.
The vapour phase being discharged from the top end 440 of the stabilizer column 400 is passed to the overhead compressor system 320 where it is compressed to an auxiliary pressure. The compressed vapour phase may optionally also be de-superheated in the overhead compressor system 320. A compressed overhead vapour stream is discharged from the overhead compressor system 320. The auxiliary pressure is higher than the feed pressure. In one example, the auxiliary pressure is 62 bara.
The step of compressing the vapour phase in the overhead compressor system 320 may, as illustrated in
Suitably, each of the overhead part streams are de-superheated by passing each of the overhead part streams through a de-superheater heat exchanger whereby at least one de-superheater heat exchanger is provided per overhead part stream.
All of the overhead part streams are recombined to form the compressed overhead vapour stream that is passed through the ambient heat exchanger 340. Prior to being passed through the ambient heat exchanger 340, but subsequent to de-superheating, the temperature of the compressed overhead vapour stream is preferably between 50° C. and 80° C. Particularly in case of surge recycle lines being provided around the overhead compressors, it is important that the de-superheated streams are guaranteed to be above dew point. Hence, it is recommended to avoid de-superheating to below 50° C.
The compressed overhead vapour stream is then passed through the ambient heat exchanger 340. At the same time, an ambient stream is passed through the ambient heat exchanger 340, in indirect heat exchanging contact with the compressed overhead vapour stream. Hereby heat is allowed to pass from the compressed overhead vapour stream to the ambient stream, as a result of which the compressed overhead vapour stream is partially condensed whereby the compressed overhead vapour stream becomes a partially condensed overhead stream at a second temperature. The ambient stream as it passes into the ambient heat exchanger 340 is at an ambient temperature prior to said indirect heat exchanging contact with the compressed overhead vapour stream. The second temperature is higher than the first temperature. The second temperature is below the dew point of the compressed overhead vapour stream at the auxiliary pressure, and above the temperature at which the ambient stream is fed into the ambient heat exchanger 340. Typically, the second temperature is in a second temperature range of from 0° C. to 20° C.
The partially condensed overhead stream is passed into the overhead separator 350, where it is separated in the vapour effluent stream and the overhead liquid stream. The vapour effluent stream is discharged from the overhead separator 350. The overhead liquid stream is also discharged from the overhead separator 350, and subsequently selectively divided into the liquid reflux stream 415 and the liquid effluent stream 215. The liquid reflux stream 415 is expanded to the feed pressure, and fed at the feed pressure into the stabilizer column 400 via the second inlet device 420. The liquid reflux stream contacts with a vapour part of the mixed phase pressurized unstabilized hydrocarbon stream 240 in the second vapour/liquid contacting device 450 within the stabilizer column 400.
Heat from the heat source 490 is preferably added to the bottom end 460 of the stabilizer column 400, below the first vapour/liquid contacting device 470. This heat may be furnished from a reboiler. The liquid phase comprising the stabilized hydrocarbon condensate being discharged from the bottom end 460 of the stabilizer column 400 is preferably cooled in condensate cooler 455, whereby heat is discharged from the liquid phase. The liquid phase thereby becomes a cooled stream comprising the stabilized hydrocarbon condensate. In a preferred embodiment, the cooled stream comprising the stabilized hydrocarbon condensate is split in the condensate splitter 454 into a recycle stream and a discharge stream. The discharge stream can then be passed to the condensate storage tank 265. The recycle stream on the other hand, can be pumped in pump 457 up to above the first vapour/liquid contacting device 470 and below the first inlet device 410. The recycle stream may then be fed back into the stabilizer column 400 at a level above the first vapour/liquid contacting device 470 and below the first inlet device 410, and at a first flow rate.
A second flow rate may be determined of the pressurized liquid hydrocarbon feed stream 251 being discharged from the inlet separator 360. The first flow rate is suitably adjusted, whereby the sum of the first flow rate and the second flow rate exceeds a pre-determined minimum liquid feed rate into the stabilizer column 400.
The partially evaporating of the pressurized unstabilized hydrocarbon condensate stream 210 in the evaporator 310 preferably comprises indirectly heat exchanging the pressurized unstabilized hydrocarbon condensate stream 210 in the feed-effluent heat exchanger against at least one of the effluent streams being fed to the feed-effluent heat exchanger at the second temperature. The effluent stream at said second temperature consists of one or both of the vapour effluent stream 290 and the liquid effluent stream 215. The vapour effluent stream 290 being discharged from the overhead separator 350 may thus advantageously be passed to the feed-effluent heat exchanger, suitably via the pressure controlled valve 298. In addition thereto or instead thereof, the liquid effluent stream 215 may be passed to the feed-effluent heat exchanger, suitably via flow regulating valve 218.
The effluent stream 230 being discharged from the feed-effluent heat exchanger is advantageously recombined with the lean pressurized refrigerated natural gas stream 30. This is done prior to said further refrigerating, such that the resulting lean pressurized refrigerated natural gas stream 35 which includes the original lean pressurized refrigerated natural gas stream 30 and the effluent stream 230 are further refrigerated together. This can be done because there are abundant volatile components (notably methane and any volatile inert components) in the pressurized unstabilized hydrocarbon condensate stream 210 being fed into the hydrocarbon condensate stabilizer 200. The molar flow rate of the effluent stream is preferably not more than 15% of the molar flow rate of the resulting lean pressurized refrigerated natural gas stream 35. Under typical conditions, the molar flow rate of the effluent stream may be between 5% and 15% of the molar flow rate of the resulting lean pressurized refrigerated natural gas stream 35.
The hydrocarbon condensate stabilizer 200 has been modeled in SimSci Pro/II to demonstrate its merits. Two cases are presented below, an average gas average ambient case (AGAA) and a rich gas cold ambient case (RGCA). The temperature of the ambient stream entering the ambient heat exchanger 340 was assumed to be 10° C. in the average ambient case, and 4° C. in the cold ambient case. Additionally, the AGAA case has been simulated at 50% turndown. In all cases the Reid vapour pressure of the stabilized hydrocarbon condensate was 0.80 bara.
Table 1 shows the composition, temperature and pressure of the partially condensed natural gas stream 20, the pressurized unstabilized hydrocarbon condensate stream 210, the vapour phase being discharged from the stabilizer column 400 in vapour discharge line 270, and of the liquid phase in liquid discharge line 250, in the AGAA case for
The pressure and temperature of the compressed overhead vapour stream 280 downstream of the de-superheater but upstream of the ambient heat exchanger 340 are 62 bar and 70° C. The dew point of the vapour phase being discharged from the stabilizer column 400 changes from 12° C. to 55° C. as a result of the compression. In the AGAA case, a recycle flow of the recycle stream from the stabilized hydrocarbon condensate is pumped up through condensate recycle line 451, and fed back into the stabilizer column at a level above the first vapour/liquid contacting device 470 and below the first inlet device 410.
For comparison, Table 2 below shows the composition, temperature and pressure of the partially condensed natural gas stream 20, the pressurized unstabilized hydrocarbon condensate stream 210, the vapour phase being discharged from the stabilizer column 400 in vapour discharge line 270, and of the liquid phase in liquid discharge line 250, in the RGCA case for
The pressure and temperature of the compressed overhead vapour stream 280 downstream of the de-superheater but upstream of the ambient heat exchanger 340 are 62 bar and 70° C. The dew point of the vapour phase being discharged from the stabilizer column 400 changes from −8° C. to 26° C. as a result of the compression.
Table 3 below repeats the simulation for the same gas composition and ambient temperature as the AGAA case, but at 50% of the flow rate. The pressure and temperature of the compressed overhead vapour stream 280 downstream of the de-superheater but upstream of the ambient heat exchanger 340 are the same as in the AGAA case. The dew point of the vapour phase being discharged from the stabilizer column 400 changes from 20° C. to 65° C. as a result of the compression. The recycle flow rate of the
recycle stream from the stabilized hydrocarbon condensate through condensate recycle line 451 was higher than in the AGAA case in order to maintain sufficient liquid loading to operate the stabilizer column 400. The dew point increases slightly in comparison to AGAA case.
The presently proposed hydrocarbon condensate stabilizer 200 can be employed with any type of natural gas liquefaction process or train. Examples of suitable liquefaction processes or trains may employ single refrigerant cycle processes (usually single mixed refrigerant—SMR—processes, such as PRICO described in the paper “LNG Production on floating platforms” by K R Johnsen and P Christiansen, presented at Gastech 1998 (Dubai). Also possible is a single component refrigerant such as for instance the BHP-cLNG process which is also described in the afore-mentioned paper by Johnsen and Christiansen). Other examples employ double refrigerant cycle processes (for instance the much applied Propane-Mixed-Refrigerant process, often abbreviated C3MR, such as described in for instance U.S. Pat. No. 4,404,008, or for instance double mixed refrigerant—DMR—processes of which an example is described in U.S. Pat. No. 6,658,891, or for instance two-cycle processes wherein each refrigerant cycle contains a single component refrigerant). Still other processes or trains are based on three or more compressor trains for three or more refrigeration cycles of which an example is described in U.S. Pat. No. 7,114,351.
Additional specific examples of liquefaction processes and trains are described in: U.S. Pat. No. 5,832,745 (Shell SMR); U.S. Pat. Nos. 6,295,833; 5,657,643 (both are variants of Black and Veatch SMR); U.S. Pat. No. 6,370,910 (Shell DMR). Another suitable example of DMR is the so-called Axens LIQUEFIN process, such as described in for instance the paper entitled “LIQUEFIN: AN INNOVATIVE PROCESS TO REDUCE LNG COSTS” by P-Y Martin et al, presented at the 22nd World Gas Conference in Tokyo, Japan (2003). Other suitable three-cycle processes include for example U.S. Pat. No. 6,962,060; US 2011/185767; U.S. Pat. No. 7,127,914; AU4349385; U.S. Pat. No. 5,669,234 (commercially known as optimized cascade process); U.S. Pat. No. 6,253,574 (commercially known as mixed fluid cascade process); U.S. Pat. No. 6,308,531; US application publication 2008/0141711; Mark J. Roberts et al “Large capacity single train AP-X™ Hybrid LNG Process”, Gastech 2002, Doha, Qatar (13-16 Oct. 2002).
Other possibilities include so-called parallel mixed refrigerant processes, such as described for instance in U.S. Pat. No. 6,389,844 (Shell PMR process), US Patent application publication Nos. 2005/005635, 2008/156036, 2008/156037, or Pek et al in “LARGE CAPACITY LNG PLANT DEVELOPMENT” 14th International Conference on Liquefied Natural Gas, Doha, Qatar (21-24 Mar. 2004); or full dependent or independent natural gas liquefaction trains such as described in for instance U.S. Pat. No. 6,658,892; or single trains comprising multiple parallel main cryogenic heat exchangers such as described in for instance U.S. Pat. No. 6,789,394, US Patent pre-grant publication No. 2007/193303, or by Paradowski et al in “An LNG train capacity of 1 BSCFD is a realistic objective”, Presented at GPA European Chapter Annual Meeting, Barcelona, Spain (27-29 Sep. 2000).
These suggestions are provided to demonstrate wide applicability of the invention, and are not intended to be an exclusive and/or exhaustive list of possibilities.
The person skilled in the art will understand that the present invention can be carried out in many various ways without departing from the scope of the appended claims.
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| PCT/EP2015/065692 | 7/9/2015 | WO | 00 |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO2016/012250 | 1/28/2016 | WO | A |
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| Number | Date | Country | |
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| 20170191748 A1 | Jul 2017 | US |
