CN100436988C - Liquefied natural gas processing - Google Patents
Liquefied natural gas processing Download PDFInfo
- Publication number
- CN100436988C CN100436988C CNB2005800147024A CN200580014702A CN100436988C CN 100436988 C CN100436988 C CN 100436988C CN B2005800147024 A CNB2005800147024 A CN B2005800147024A CN 200580014702 A CN200580014702 A CN 200580014702A CN 100436988 C CN100436988 C CN 100436988C
- Authority
- CN
- China
- Prior art keywords
- logistics
- flow
- stream
- tower
- make
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
A process and apparatus for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbons from a liquefied natural gas (LNG) stream is disclosed. The LNG feed stream is divided into two portions. The first portion is supplied to a fractionation column at an upper mid-column feed point. The second portion is directed in heat exchange relation with a warmer distillation stream rising from the fractionation stages of the column, whereby this portion of the LNG feed stream is partially heated and the distillation stream is totally condensed. The condensed distillation stream is divided into a 'lean' LNG product stream and a reflux stream, whereupon the reflux stream is supplied to the column at a top column feed position. The partially heated portion of the LNG feed stream is heated further to partially or totally vaporize it and thereafter supplied to the column at a lower mid-column feed position. The quantities and temperatures of the feeds to the column are effective to maintain the column overhead temperature at a temperature whereby the major portion of the desired components is recovered in the bottom liquid product from the column.
Description
Technical field
The present invention relates to a kind of from liquefied natural gas (hereinafter being called LNG), separate ethane and more heavy hydrocarbon or propane and more heavy hydrocarbon the natural gas liquid (NGL) (NGL) of poor LNG logistics of volatile methane rich and low volatility or the method for liquefied petroleum gas (LPG) logistics are provided.The applicant requires formerly U.S. Provisional Application number 60/584 according to the 35th piece the 119th of United States Code joint (e), 668 (applications on July 1st, 2004), 60/646,903 (applications on January 24th, 2005), 60/669, the rights and interests of 642 (applications on April 8th, 2005) and 60/671,930 (application on April 15th, 2005).
Background technology
As the alternative that pipeline is carried, backwoodsman natural gas to be liquefied and in special-purpose LNG jar, be transported to suitable LNG sometimes and receive and store the tank field.LNG is vaporized again and by the mode identical with natural gas as fuel gas.Although LNG has the methane of larger proportion usually, namely for methane accounts at least 50% (mole) of LNG, also contains a small amount of heavy hydrocarbon and nitrogen such as ethane, propane and butane etc.Usually need make some or all of heavy hydrocarbons among the LNG and methane separation so that LNG vaporization gained gaseous fuel meets the requirement of pipeline gas calorific value.In addition, because heavy hydrocarbon as its value height that acts as a fuel of value ratio of product liquid (for example as petrochemical material), also wishes to make these heavy hydrocarbons and methane separation usually.
Although can be used to from LNG to separate ethane and more the method for heavy hydrocarbon is a lot, these methods must be dealt carefully with the relation between high-recovery, low public work expense and the technology simple (thereby small investment) usually.US 2,952, and 984,3,837,172 and 5,114,451 and application No.10/675 co-pending simultaneously, 785 have described relevant LNG method, reclaiming the poor LNG logistics that ethane or propane produce gaseous state simultaneously, then the latter are compressed to discharge pressure and enter gas distribution mesh.Yet, producing liquid poor LNG logistics if change into, public work is taken may be lower, can make poor LNG vaporization with a spot of external heat source or other means subsequently with it with the discharge pressure of pump pressure (but not compression) to gas distribution mesh.U.S. Patent Application Publication No. US 2003/0158458A1 has described the method.
Summary of the invention
Broad sense of the present invention relates to the method that reclaims ethene, ethane, propylene, propane and heavy hydrocarbon from such LNG logistics.Adopt new technology arrangement to make ethane or propane recovery height keep the simple and small investment of process equipment simultaneously.In addition, the present invention also makes the required public work of processing LNG (electricity and heat) minimizing cause operating cost lower than prior art method.The canonical analysis result of the LNG logistics that will handle by the present invention is (approximate molar percentage) 86.7% methane, 8.9% ethane and other C
2Component, 2.9% propane and other C
3Component, 1.0% butane+and the nitrogen of surplus.
Description of drawings
For understanding the present invention better, with reference to following examples and accompanying drawing.Referring to accompanying drawing:
Fig. 1 is the flow chart of prior art LNG treatment facility;
Fig. 2 is the flow chart according to the prior art LNG treatment facility of U.S. Patent Application Publication No. US2003/0158458A1;
Fig. 3 is the flow chart according to LNG treatment facility of the present invention; With
Fig. 4 to 13 is flow charts of the optional mode of explanation LNG treatment facility of the present invention.
Below in the explanation to above-mentioned accompanying drawing, the flow summary sheet that calculates at the typical process condition is provided.For simplicity, in these tables that this paper occurs, flow value (mole/hour) has been rounded to immediate integer.Total logistics flux shown in the table comprises that all non-hydrocarbons components thereby general meeting are greater than hydrocarbon component logistics flux sum.Shown in temperature be the approximation that has rounded up.Should also be noted that the technological design of carrying out for method shown in the comparison diagram is that (perhaps from process to environment) do not have the basis of heat loss to calculate from environment to process in supposition.The quality that is purchased insulating materials makes it to become quite reasonable supposition and is the supposition that those skilled in the art adopt usually.
For simplicity, with traditional English unit and international (S I) unit report technological parameter of making.In the table given molar flow may be interpreted as pound molecule/hour or kilomol/hour.Corresponding with the energy consumption of horsepower (HP) and/or thousand British thermal units/hour (MBTU/Hr) report with described molar flow with pound molecule/hour be unit.Corresponding with the energy consumption of kilowatt report with described molar flow with kilomol/hour be unit.
The specific embodiment
Prior art
Referring to Fig. 1, in order to compare, we are fit to production from an example and comprise the most of C that exists the raw material
2Component reaches more, and the prior art LNG treatment facility of the NGL product of heavy hydrocarbon component begins.Pending LNG (logistics 41) from LNG jar 10 enters pump 11 under-255 °F [159 ℃].Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters separator 15 then.The logistics 41a that discharges from this pump carries out heat exchange by the domethanizing column tower bottom liquid product (logistics 51) with the air-flow 52 of-120 [84 ℃] and 80 [27 ℃] and is heated in heat exchanger 12 and 13.
Still or tower 21 (being commonly referred to domethanizing column) are the column plate, one or more packed bed or the column plate that comprise a plurality of perpendicular separations and the conventional destilling tower of certain combination of filler.Column plate and/or filler make between the steam of the liquid that descends in the tower and rising contacting of necessity are taken place.This tower also comprises one or more reboiler (as reboiler 25), the stripping steam that the liquid that a part flows downward along tower can be heated and vaporizes and upwards flow along tower to provide.These steam collection come out methane stripping from liquid, thereby make tower bottom liquid product (logistics 51) not contain methane substantially but by most of C contained in the LNG incoming flow
2Component and heavy hydrocarbon are formed.(, needing high level public work thermal source to give reboiler heat supply, for example used heat medium in this example usually) owing to require temperature range in this tower reboiler.Specification according to methane volume fraction in the tower bottom product is generally 0.005, and liquid product stream 51 is at the bottom of leaving tower under 80 °F [27 ℃].Be cooled to 43 °F [6 ℃] as previously described afterwards in heat exchanger 13, product liquid (logistics 51a) flows into storage tank or further handles.
The logistics flux of method shown in Figure 1 and energy consumption gather and are shown in the following table:
Table I
(Fig. 1)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
Fig. 2 illustrates according to U.S. Patent Application Publication No. US 2003/0158458A1 a kind of alternative process earlier, and used in can obtaining than Fig. 1 under lower public work consumption condition have the high slightly rate of recovery of process earlier.The method of Fig. 2 is fit to production and comprises the most of C that exists in the feed stream
2Component reaches the more NGL product of heavy hydrocarbon component, has been applied to LNG composition and condition and prior figures 1 described identical process.
In the simulation process of Fig. 2 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters fractionating column 21 then.The logistics 41a that discharges from this pump carries out heat exchange with the domethanizing column tower bottom liquid product (logistics 51) of the compressed vapour stream 52a of the vapor stream of top of the tower 48 of-130 [90 ℃] ,-122 [86 ℃] and 85 [29 ℃] and is heated in heat exchanger 12 and 13.Partly the logistics 41c of heating further is heated to-120 °F [84 ℃] (logistics 41d) with low-lying level public work heat in heat exchanger 14 then.(high level public work heat is more expensive than low-lying level public work heat usually, so use low-lying level heat to use high level heat as the used seawater of this example substantially, can reach the purpose that reduces operating cost usually with minimizing.) after logistics 41e is expanded to the operating pressure (about 450psia[3,103kPa (a)]) of fractionating column 21 through control valve 20, at-123 [86 ℃] feed points at inflow tower middle part down.
Domethanizing column is the column plate, one or more packed bed or the column plate that comprise a plurality of perpendicular separations and the conventional destilling tower of certain combination of filler in the tower 21.As situation common in the natural gas processing equipment, described fractionating column can constitute by two sections.Top absorbs (rectifying) section 21a and comprises and can provide necessary column plate that contacts and/or filler so that condensation and absorption ethane and heavy ends between the cold liquid with descending for the rising steam; Bottom stripping (demethanation) section 21b comprises can provide necessary column plate that contacts and/or filler between dropping liq and the rising steam.The demethanation section also comprises one or more reboiler (as reboiler 25), the liquid heating that a part can be flowed downward along tower and make it to vaporize the stripping steam that upwards flows along tower is provided.These steams stripping from liquid goes out methane, thereby makes tower bottom liquid product (logistics 51) not contain methane substantially but by contained most of C in the LNG feed stream
2Component and heavy hydrocarbon are formed.
Discharge liquid product stream 51 bottom from fractionating column 21 under 85 [29 ℃], is 0.005 based on methane volume fraction in the tower bottom product.Product liquid (logistics 51a) is cooled to 0 °F [18 ℃] and flows into storage tank or further processing afterwards in aforesaid heat exchanger 13.The methane rich residual gas (logistics 52) that leaves reflux splitter 26 is compressed to 493psia[3 with compressor 27 (external power driving), 400kPa (a)] (logistics 52a), so that this logistics all condensations when in aforesaid heat exchanger 12, being cooled to-136 [93 ℃].Use pump 32 that condensate liquid (logistics 52b) is pressurized to 1365psia[9 then, 411kPa (a)] (logistics 52c) be used for follow-up vaporization and/or course of conveying.
The logistics flux of method shown in Figure 2 and energy consumption gather and are shown in the following table:
Table II
(Fig. 2)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
Have the shown rate of recovery of Table II of process and the shown rate of recovery of Table I that Fig. 1 has process earlier to compare earlier top Fig. 2, Fig. 2 method can obtain the essentially identical ethane recovery and high slightly propane and butane+rate of recovery.Public work consumption in the Table II and the contrast in the Table I show: all will the lacking of the electric power of Fig. 2 method needs and high level public work ratio of specific heat Fig. 1 method.Adopt the method for reflux operations in this tower, more effectively to reclaim ethane by domethanizing column 21 in Fig. 2 method and thereby heavy ends reach the purpose that reduces electric power.This allows the tower feeding temperature higher than Fig. 1 method again, by reduced the demand for heat (using high level public work heat) of reboiler in the domethanizing column 21 with the method for this tower charging of low-lying level public work heat heating in heat exchanger 14.(annotate: Fig. 1 method bottoms product steam 51a is cooled to 43 °F [6 ℃], and Fig. 2 method then is comparatively ideal 0 °F [18 ℃].For Fig. 1 method, attempt to make logistics 51a to be cooled to the high level public work caloric requirement that low temperature has more reduced reboiler 25 really, but the logistics 41c temperature that can cause entering separator 15 is higher and the power consumption of Pistonless compressor 27 is disproportionately increased, because will keep the operating pressure that enough rate of recovery must reduce separator 15.)
Detailed Description Of The Invention
Fig. 3 illustrates the flow chart of a method according to the present present invention.Identical among the LNG composition that sets in the method shown in Figure 3 and condition and Fig. 1 and 2.Therefore, Fig. 3 method can compare with the method for Fig. 1 and 2 so that advantage of the present invention to be described.
In the simulation process of Fig. 3 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters separator 15 then.The logistics 41a separated into two parts- logistics 42 and 43 of from this pump, discharging.First's (logistics 42) infeeds this tower by operating pressure (about 450psia[3,103kPa (a)]) and the feed points at first tower middle part that expansion valve 17 is expanded to fractionating column 21.Second portion (logistics 43) was heated before entering separator 15 and makes it all or part of vaporization.In embodiment illustrated in fig. 3, logistics 43 is heated to-106 °F [77 ℃] by the reflux stream 53 by the compression overhead gas stream 48a that makes-112 [80 ℃] ,-129 [90 ℃] in heat exchanger 12 and 13 with from the method for product liquid (logistics 51) cooling of 85 [29 ℃] of described tower earlier.The logistics 43b that will partly heat with low-lying level public work heat in heat exchanger 14 further heats (logistics 43c) then.Attention: under all situations, heat exchanger 12,13 and 14 can be represented a plurality of mono heat exchangers or single multi-path heat exchange device or its any combination.(as for how determining that specifying firing equipment is then to depend on a number of factors with one or more heat exchanger, includes but not limited to LNG input flow rate, heat exchanger size, stream temperature etc.)
Domethanizing column is the conventional destilling tower of certain combination of the column plate, one or more packed bed or column plate and the filler that comprise a plurality of perpendicular separations in the fractionating column 21.Similar with fractionating column shown in Figure 2, the fractionating column among Fig. 3 can constitute by two sections.Top absorbs (rectifying) section and comprises and can provide necessary column plate that contacts and/or filler so that condensation and absorption ethane and heavy ends between the cold liquid with descending for the rising steam; Bottom stripping (demethanation) section comprises can provide necessary column plate that contacts and/or filler between dropping liq and the rising steam.The demethanation section also comprises one or more reboiler (as reboiler 25), the stripping steam that the liquid that a part flows downward along tower can be heated and makes it to vaporize and make progress and flow along tower to provide.Liquid product stream 51 is 0.005 discharging at the bottom of tower under 85 °F [29 ℃] based on methane volume fraction in the tower bottom product.Product liquid (logistics 51a) is cooled to 0 [18 ℃] back as previously described and flows into storage tank or further processing in heat exchanger 13.
Cat head distillates air-flow 48 and discharges and flow into by decompressor 18 compressor driven 19 from the top of fractionating column 21 under-134 °F [92 ℃], is compressed into 550psia[3 therein, 789kPa (a)] (logistics 48a).Under this pressure, whole condensations when this logistics is cooled to-129 [90 ℃] in aforesaid heat exchanger 12.Make condensate liquid (logistics 48b) separated into two parts (logistics 52 and 53) then.First's (logistics 52) is the poor LNG logistics of methane rich, and it is pressurized to 1365psia[9 by pump 32,411kPa (a)] (logistics 52a) be used for follow-up vaporization and/or course of conveying.
Another part is a reflux stream 53, and its inflow heat exchanger 12 made it to be chilled to-166 °F [110 ℃] by carrying out heat exchange with the cold LNG of a part (logistics 43) as previously described.Cross cold reflux stream 53a and be expanded to the operating pressure of domethanizing column 21 by expansion valve 30, the logistics 53b of Peng Zhanging infeeds domethanizing column 21 as cold cat head charging (phegma) then.This cold reflux liquid absorbs and condensation C from the steam that rises in the upper rectifying section of domethanizing column 21
2Component reaches more heavy hydrocarbon component.
The logistics flux of method shown in Figure 3 and energy consumption gather and are shown in the following table:
Table III
(Fig. 3)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
The Fig. 1 that shows in Fig. 3 method rate of recovery that shows in the last Table III and the Table I has the rate of recovery contrast of process to show earlier: ethane recovery of the present invention and Fig. 1 suitable and propane recovery (99.89% pair 98.33%) and butane+rate of recovery (100.00% pair 99.62%) are higher slightly than Fig. 1's.But public work consumption in the Table III and the contrast in the Table I show: electric power required for the present invention and high level public work ratio of specific heat Fig. 1 method much lower (reducing 26% and 64% respectively).
Fig. 2 has the rate of recovery contrast of process to show earlier among the rate of recovery that shows in the Table III and the Table I I: the rate of recovery of liquids recovery rate of the present invention and Fig. 2 method is (having only propane recovery lower slightly, 99.89% pair 100.00%) substantially quite.But public work consumption in the Table III and the contrast in the Table II show: electric power required for the present invention and high level public work heat are starkly lower than Fig. 2 method (reducing 11% and 53% respectively).
Three principal elements that cause efficiency improvement of the present invention are arranged.The first, there is process to compare earlier with Fig. 1, the present invention does not rely on LNG charging itself directly as the phegma of fractionating column 21, produces a wherein desire recovery C but the refrigeration that cold LNG is intrinsic is used for heat exchanger 12
2Component and the few reflux stream (logistics 53) of heavy hydrocarbon constituent content more make in the top absorber portion of fractionating column 21 more effectively rectifying and have avoided Fig. 1 that the equilibrium-limited of process is arranged earlier.The second, compare with the process that has earlier of Fig. 1 and 2, before infeeding fractionating column 21, make LNG charging separated into two parts can more effectively utilize low-lying level public work heat, thus the amount of the high level public work heat that minimizing reboiler 25 is consumed.Colder that part of LNG charging (logistics 42a among Fig. 3) makes the steam in expanded gas flow and the liquid stream ( logistics 46a and 47a among Fig. 3) carry out part rectifying so that the operation of the heating and this partial L NG charging (logistics 43) of partly vaporizing can excessively not increase the condensation load of heat exchanger 12 as the reflux stream of adding of fractionating column 21.The 3rd, compare with the process that has earlier of Fig. 2, as adding reflux stream used fractionating column 21 overhead reflux amounts are reduced with a part of cold LNG charging (logistics 42a among Fig. 3), as the 53 contrast findings of logistics in logistics in the Table III 53 and the Table II.The overhead reflux flow quantity reduces, add the degree with the heating of low-lying level public work heat big (as Table III and Table II contrast finding) in the heat exchanger 14, the total amount of liquid that causes entering fractionating column 21 reduces, and reboiler 25 required loads reduce and the amount that satisfies the required high level public work heat of domethanizing column tower bottom liquid product specification is minimized.
Fig. 4 illustrates a kind of alternative embodiment of the present invention.Among the LNG composition of setting in the method shown in Figure 4 and condition and Fig. 3 and front Fig. 1 and 2 described identical.Therefore, Fig. 4 method of the present invention can contrast with process is arranged earlier shown in embodiment shown in Figure 3 and Fig. 1 and 2.
In the simulation process of Fig. 4 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters separator 15 then.The logistics 41a that discharges from this pump was heated before entering separator 15 and makes it all or part of vaporization.In embodiment illustrated in fig. 4, logistics 41a earlier is heated to-99 °F [73 ℃] by cooling off with the reflux stream 53 of the compression overhead gas stream 48b of-63 [53 ℃] ,-135 [93 ℃] with from the product liquid (logistics 51) of 85 [29 ℃] of described tower in heat exchanger 12 and 13.The logistics 41c that will partly heat with low-lying level public work heat in heat exchanger 14 further heats (logistics 41d) then.
Steam (logistics 44) from separator 15 is divided into two bursts of logistics 45 and 46.Heat exchanger 16 is passed in the logistics 45 that comprises described total steam about 30%, carries out heat exchange with the cold steam of demethanizer column overhead (logistics 48) of-134 [92 ℃], is cooled to basic condensation.Then the basic condensate flow 45a of-129 [89 ℃] of gained is expanded to the operating pressure of fractionating column 21 by expansion valve 17 flash distillations.Part logistics vaporization in the expansion process causes total logistics cooling.In the method shown in Figure 4, the expansion logistics 45b that leaves expansion valve 17 reaches the temperature of-133 [92 ℃], infeeds fractionating column 21 at first tower middle part feed points.
All the other steams from separator 15 of 70% (logistics 46) enter work done decompressor 18, take out mechanical energy from this part high pressure charging.Decompressor 18 makes steam expand substantially isentropically to the operating pressure of tower, and described work done expansion process makes expansion logistics 46a be cooled to the temperature of-90 [68 ℃] approximately.The expanded gas flow 46a of partial condensation infeeds fractionating column 21 as charging at tower middle part feed points then.
Cat head distillate that air-flow 48 is discharged from the top of fractionating column 21 under-134 °F [92 ℃] and heat exchanger 16 with reverse the passing through of feeding gas of input, be heated to-78 °F [61 ℃] therein.Logistics 48a after the heating flows into by decompressor 18 compressor driven 19, is compressed into 498psia[3 therein, 430kPa (a)] (logistics 48b).Under this pressure, whole condensations when this logistics is cooled to-135 [93 ℃] as previously described in heat exchanger 12.Make condensate liquid (logistics 48c) separated into two parts (logistics 52 and 53) then.First's (logistics 52) is the poor LNG logistics of methane rich, is pressurized to 1365psia[9 by pump 32,411kPa (a)] (logistics 52a) be used for follow-up vaporization and/or course of conveying.
Another part is a reflux stream 53, and its inflow heat exchanger 12 made it to be chilled to-166 °F [110 ℃] by carrying out heat exchange with cold LNG (logistics 41a) as previously described.Cross cold reflux stream 53a and be expanded to the operating pressure of domethanizing column 21, then the logistics 53b that expands is infeeded domethanizing column 21 as cat head cold feed (phegma) by expansion valve 30.This cold reflux liquid absorbs and condensation C from the steam that rises in the upper rectifying section of domethanizing column 21
2Component reaches more heavy hydrocarbon component.
The logistics flux of method shown in Figure 4 and energy consumption gather and are shown in the following table:
Table IV
(Fig. 4)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
The Table III contrast of the Table IV of top Fig. 4 embodiment of the present invention and Fig. 3 embodiment of the present invention shows: the liquids recovery rate of Fig. 4 embodiment is basic identical.Since Fig. 4 embodiment utilize overhead (logistics 48) in heat exchanger 16 with a part of steam (logistics 45) condensation of separator 15 and cold excessively produce fractionating column 21 add phegma (logistics 45b), so it is high more a lot of than the temperature of the corresponding logistics (logistics 48) of Fig. 3 embodiment to enter the gas (logistics 48a) of compressor 19.According to the compressor reducer type that this equipment adopted, temperature is higher can to provide advantage at aspects such as metallurgy.But because infeed fractionating column 21 to add reflux stream 45b cold not as logistics 42a in Fig. 3 embodiment, can use the low-lying level public work heat of less amount in the heat exchanger 14 so need more overhead reflux liquid (logistics 53b).This can make the load of reboiler 25 increase and the amount of the required high level public work of Fig. 4 embodiment of the present invention heat is increased than Fig. 3 embodiment.The overhead reflux flow quantity also makes the electric power requirement of Fig. 4 embodiment than Fig. 3 embodiment high slightly (about 2%) greatly.Select to adopt which kind of embodiment generally to depend on the relative cost of electric power and high level public work heat and the counter investment expense of pump, heat exchanger and compressor in concrete the application.
Embodiment 3
Fig. 5 illustrates a kind of simpler alternative embodiment of the present invention.In the LNG composition of setting in the method shown in Figure 5 and condition and Fig. 3 and 4 and front Fig. 1 and 2 described identical.Therefore, Fig. 5 method of the present invention can contrast with process is arranged earlier shown in embodiment shown in Fig. 3 and 4 and Fig. 1 and 2.
In the simulation process of Fig. 5 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters separator 15 then.The logistics 41a that discharges from this pump was heated before entering separator 15 and makes it all or part of vaporization.In embodiment illustrated in fig. 5, logistics 41a is the reflux stream 53 by the compression overhead gas stream 48a that makes-110 [79 ℃] ,-128 [89 ℃] and be heated to-102 [75 ℃] from product liquid (logistics 51) cooling of 85 [29 ℃] of described tower in heat exchanger 12 and 13 earlier.The logistics 41c that will partly heat with low-lying level public work heat in heat exchanger 14 further heats (logistics 41d) then.
Cat head distillates air-flow 48 and discharges and flow into by decompressor 18 compressor driven 19 from the top of fractionating column 21 under-134 °F [92 ℃], is compressed into 563psia[3 therein, 882kPa (a)] (logistics 48a).Under this pressure, whole condensations when this logistics is cooled to-128 [89 ℃] as previously described in heat exchanger 12.Make condensate liquid (logistics 48b) separated into two parts (logistics 52 and 53) then.First's (logistics 52) is the poor LNG logistics of methane rich, and it is pressurized to 1365psia[9 by pump 32,411kPa (a)] (logistics 52a) be used for follow-up vaporization and/or course of conveying.
Another part is a reflux stream 53, and its inflow heat exchanger 12 made it to be chilled to-184 °F [120 ℃] by carrying out heat exchange with cold LNG (logistics 41a) as previously described.Cross cold reflux stream 53a and be expanded to the operating pressure of domethanizing column 21 by expansion valve 30, the logistics 53b of Peng Zhanging infeeds domethanizing column 21 as cat head cold feed (phegma) then.This cold reflux liquid absorbs and condensation C from the steam that rises in the upper rectifying section of domethanizing column 21
2Component reaches more heavy hydrocarbon component.
The logistics flux of method shown in Figure 5 and energy consumption gather and are shown in the following table:
Table V
(Fig. 5)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
The Table IV contrast of the Table III of the Table V of top Fig. 5 embodiment of the present invention and Fig. 3 embodiment of the present invention and Fig. 4 embodiment shows: the liquids recovery rate of Fig. 5 embodiment is basic identical.Because not resembling Fig. 3 and 4 embodiments fractionating column 21 used, Fig. 5 embodiment do not add phegma (being respectively logistics 42a and 45b), so the amount that needs low-lying level public work heat used in more overhead reflux liquid (logistics 53b) and the heat exchanger 14 still less.This increases the load of reboiler 25 and the amount of the required high level public work of Fig. 5 embodiment of the present invention heat is increased than Fig. 3 and 4 embodiments.The higher electric power requirement of Fig. 5 embodiment that also makes of overhead reflux flow quantity is than Fig. 3 and 4 embodiments high slightly (height about 5% and 3% respectively).Select to adopt which kind of embodiment generally to depend on the relative cost of electric power and high level public work heat and the counter investment expense of tower, pump, heat exchanger and compressor in concrete the application.
Embodiment 4
Adopt as shown in Figure 6 another embodiment of the present invention can obtain a kind ofly can under the low energy consumption condition, keep same C
2The more complicated design of the summary of component recovery.Among the LNG composition of setting in the method shown in Figure 6 and condition and Fig. 3 to 5 and front Fig. 1 and 2 described identical.Therefore, Fig. 6 method of the present invention can contrast with process is arranged earlier shown in embodiment shown in Fig. 3 to 5 and Fig. 1 and 2.
In the simulation process of Fig. 6 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters absorption tower 21 then.In embodiment illustrated in fig. 6, the logistics 41a that discharges from this pump earlier heat exchanger 12 by making-129 [90 ℃] overhead vapours (distillating air-flow 48) of in contact separation device absorptive tower 21, discharging and being heated to-120 °F [84 ℃] from-83 [63 ℃] overhead vapours (distillating air-flow 50) cooling that fractionation stripper 24 is discharged.The liquid of part heating flows 41b separated into two parts (logistics 42 and 43) then.First's (logistics 42) is expanded to the operating pressure (about 495psia[3,413kPa (a)]) on absorption tower 21 and infeeds this tower at second tower middle part feed points by expansion valve 17.
Second portion (logistics 43) was heated before entering absorption tower 21 and makes it all or part of vaporization.In embodiment illustrated in fig. 6, logistics 43 earlier in heat exchanger 13 by making 88 [31 ℃] product liquids (logistics 51) cooling be heated to-112 °F [80 ℃] from fractionation stripper 24.Partly the logistics 43a of heating further heats (logistics 43b) with low-lying level public work heat in heat exchanger 14 then.The logistics 43b of part vaporization is expanded to the operating pressure on absorption tower 21 by expansion valve 20, makes logistics 43c be cooled to-67 °F [55 ℃], infeeds absorption tower 21 at tower underfeed point then.The liquid part (if any) of expansion logistics 43c is mixed with the liquid that 21 tops from the absorption tower fall, and mixed liquor stream 49 is the 21 bottoms discharge from the absorption tower under-79 °F [62 ℃].The gas phase of expansion logistics 43c part 21 rises and contacts condensation and absorb C with the cold liquid that falls through the absorption tower
2Component reaches more heavy hydrocarbon component.
Be expanded to the operating pressure (465psia[3 of a little higher than stripper 24 by expansion valve 22 flash distillations from the mixed liquor stream 49 of 21 bottoms, contact arrangement absorption tower, 206kPa (a)]), logistics 49 enters fractionation stripper 24 at the cat head feed points after being cooled to-83 °F [64 ℃] (logistics 49a).In stripper 24, it is 0.005 specification to satisfy the methane volume fraction that the steam stripping from logistics 49a that produces in the reboiler 25 goes out methane.Discharge gained liquid product stream 51 bottom from stripper 24 under 88 [31 ℃], is cooled to 0 °F [18 ℃] (logistics 51a) as previously described in heat exchanger 13, flows into storage tank or further processing then.
Overhead vapours (logistics 50) from stripper 24 is left this tower and inflow heat exchanger 12 under-83 °F [63 ℃], be cooled to-132 °F [91 ℃] as previously described therein, makes the whole condensations of this logistics.Condensate stream 50a enters cat head air pump 33 then, makes the pressure of logistics 50b rise to the operating pressure on a little higher than absorption tower 21.Be expanded to the operating pressure on absorption tower 21 by control valve 35 after, the logistics 50c of-130 [90 ℃] infeeds absorption tower 21 at first tower middle part feed points, and the liquid that falls with 21 tops from the absorption tower mixes to a part is used for from the absorption tower 21 bottoms and rises steam and capture C therein
2Liquid with heavy component.
Cat head distillates air-flow 48 21 top discharge from the absorption tower under-129 [90 ℃], and inflow heat exchanger 12 also is cooled to-135 °F [93 ℃] as previously described, makes the whole condensations of this logistics.Condensate liquid (logistics 48a) is pressurized to the operating pressure (logistics 48b) on a little higher than absorption tower 21, separated into two parts (logistics 52 and 53) then by pump 31.First's (logistics 52) is the poor LNG logistics of methane rich, and it is pressurized to 1365psia[9 by pump 32,411kPa (a)] (logistics 52a) be used for follow-up vaporization and/or course of conveying.
Another part is a reflux stream 53, and it is expanded to the operating pressure on absorption tower 21 by control valve 30.The logistics 53a of Peng Zhanging infeeds absorption tower 21 as cat head cold feed (phegma) under-135 °F [93 ℃] then.This cold reflux liquid absorbs and condensation C from the steam that rises in the upper rectifying section on absorption tower 21
2Component reaches more heavy hydrocarbon component.
Method logistics flux shown in Figure 6 and energy consumption are shown in the following table:
Table VI
(Fig. 6)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
The Table III of the Table VI of top Fig. 6 embodiment of the present invention and Fig. 3 to 5 embodiment of the present invention to V contrast shows: the liquids recovery rate of Fig. 6 embodiment is basic identical.But public work consumption in the Table VI and Table III to the contrast among the V shows: Fig. 6 embodiment required electric power of the present invention and high level public work heat all descend than Fig. 3 to 5 embodiment.The electric power requirement of Fig. 6 embodiment reduces by 1%, 4% and 6% respectively, and high level public work caloric requirement reduces by 1%, 4% and 20% respectively.
The utilities requirements of Fig. 6 embodiment of the present invention reduces than Fig. 3 to 5 embodiment can be mainly owing to two factors.The first, the operating pressure that the fractionating column in Fig. 3 to 5 embodiment 21 is divided into discrete absorption tower 21 and stripper 24, two towers can be optimized independently at its each self-applying.Can not to bring up to institute a lot of more than the indicating value for the operating pressure of fractionating column 21 in Fig. 3 to 5 embodiment, so just can not take place because of the adverse effect of high operating pressure to the distillation procedure generation.The phase behavior that this influence shows as because of its steam and liquid stream causes fractionating column 21 inner transmission matters relatively poor.What be concerned about especially is the physical property that influences the solution-air separative efficiency, i.e. the density contrast of surface tension of liquid and two-phase.The operating pressure of distillation operation (absorption tower 21) and stripping operation (stripper 24) no longer resembles and links together Fig. 3 to 5 embodiment, the stripping operation can reasonably carried out under the operating pressure, and distillation operation can carry out under the elevated pressures that helps its overhead gas stream (logistics 48 in Fig. 6 embodiment) condensation in heat exchanger 12 simultaneously.
Second, part LNG incoming flow is as adding the reflux stream (among Fig. 3 among logistics 42a and Fig. 4 logistics 45b) in Fig. 3 and 4 embodiments, and Fig. 6 embodiment of the present invention has also used second to add reflux stream (logistics 50c) and so that help the steam among the logistics 43c that enters 21 bottoms, absorption tower is carried out rectifying to absorption tower 21.Can in heat exchanger 14, utilize low-lying level public work heat to reduce the load of reboiler 25 so better, reduce the requirement of high level public work heat.Select to adopt which kind of embodiment generally to depend on the relative cost of electric power and high level public work heat and the counter investment expense of tower, pump, heat exchanger and compressor in concrete the application.
As shown in Figure 7, the present invention also can be used for producing and comprises the most of C that exists in the feed stream
3Component reaches the more LPG product of heavy hydrocarbon component.The LNG composition of setting in the method shown in Figure 7 is described identical with prior figures 1 to 6 with condition.Therefore, Fig. 7 method of the present invention can contrast with other embodiment of the present invention shown in process and Fig. 3 to 6 is arranged earlier shown in Fig. 1 and 2.
In the simulation process of Fig. 7 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters absorption tower 21 then.In embodiment illustrated in fig. 7, the logistics 41a that discharges from this pump is the compression overhead vapours (logistics 50a) by making-90 [68 ℃] overhead vapours (distillating air-flow 48) of discharging, 57 [14 ℃] of discharging in fractionation stripper 24 in contact separation device absorptive tower 21 and be heated to-99 [73 ℃] from 190 [88 ℃] product liquids (logistics 51) cooling of fractionation stripper 24 heat exchanger 12 and 13 earlier.
Partly the liquid of heating stream 41c uses the further heating of low-lying level public work heat (logistics 41d) to-43 [42 ℃] in heat exchanger 14 then.The logistics 41d of part vaporization is expanded to the operating pressure (about 465psia[3,206kPa (a)]) on absorption tower 21 by expansion valve 20, makes logistics 41e be cooled to-48 °F [44 ℃], infeeds absorption tower 21 at tower underfeed point then.The liquid part (if any) of expansion logistics 41e is mixed with the liquid that 21 tops from the absorption tower fall, and mixed liquor stream 49 is the 21 bottoms discharge from the absorption tower under-50 °F [46 ℃].The gas phase of expansion logistics 41e part 21 rises and contacts condensation and absorb C with the cold liquid that falls through the absorption tower
3Component and more heavy ends.
Be expanded to the operating pressure (430psia[2 of a little higher than stripper 24 by expansion valve 22 flash distillations from the mixed liquor stream 49 of 21 bottoms, contact arrangement absorption tower, 965kPa (a)]), logistics 49 is cooled to-53 °F [47 ℃] (logistics 49a), enters fractionation stripper 24 at the cat head feed points then.In stripper 24, the steam stripping from logistics 49a that produces in the reboiler 25 goes out methane and C
2Component is 0.020: 1 specification with the mol ratio that satisfies ethane and propane.Discharge gained liquid product stream 51 bottom from stripper 24 under 190 [88 ℃], is cooled to 0 °F [18 ℃] (logistics 51a) as previously described in heat exchanger 13, flows into storage tank or further processing then.
Under 30 °F [1 ℃], leave this tower and flow into tower overhead gas compressor 34 (by adding power drives) from the overhead vapours (logistics 50) of stripper 24, make the pressure of logistics 50a rise to the operating pressure on a little higher than absorption tower 21.Logistics 50a enters heat exchanger 12, is cooled to-78 °F [61 ℃] as previously described therein, makes the whole condensations of this logistics.Condensate stream 50b is expanded to the operating pressure on absorption tower 21 by control valve 35, the logistics 50c of gained-84 [64 ℃] infeeds absorption tower 21 at tower middle part feed points then, mixes to a part with the liquid that falls from 21 tops, absorption tower therein to be used for capturing C from the steam that 21 bottoms, absorption tower rise
3Reach the more liquid of heavy ends.
Cat head distillates air-flow 48 21 top discharge from the absorption tower under-90 [68 ℃], and inflow heat exchanger 12 also is cooled to-132 °F [91 ℃] as previously described, makes the whole condensations of this logistics.Condensate liquid (logistics 48a) is pressurized to the operating pressure (logistics 48b) on a little higher than absorption tower 21, separated into two parts (logistics 52 and 53) then by pump 31.First's (logistics 52) is the poor LNG logistics of methane rich, and it is pressurized to 1365psia[9 by pump 32,411kPa (a)] (logistics 52a) be used for follow-up vaporization and/or course of conveying.
Another part is a reflux stream 53, and it is expanded to the operating pressure on absorption tower 21 by control valve 30.The logistics 53a of Peng Zhanging infeeds absorption tower 21 as cat head cold feed (phegma) under-131 °F [91 ℃] then.This cold reflux liquid absorbs and condensation C from the steam that rises on the top on absorption tower 21
3Component reaches more heavy hydrocarbon component.
The logistics flux of method shown in Figure 7 and energy consumption are shown and are summarized in the following table:
Table VII
(Fig. 7)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
Public work consumption and Table III to the contrast of VI shows in the Table VII of top Fig. 7 method: the electric power requirement of this embodiment of the present invention is higher slightly than Fig. 3 to 6 embodiment.But the obvious reduction of the required high level public work of Fig. 7 embodiment of the present invention ratio of specific heat Fig. 3 to 6 embodiment is not because ought want to reclaim C
2During component, then there is more low-lying level public work heat to be used for heat exchanger 14.
Embodiment 6
The electric power requirement of Fig. 7 embodiment of the present invention mainly is because the compressor 34 among Fig. 7 than the increase of Fig. 3 to 6 embodiment, and it provides the overhead vapours (logistics 50) that makes from stripper 24 to enter the required power in absorption tower 21 then by heat exchanger 12.Fig. 8 illustrates a kind of alternative embodiment of the present invention, has wherein cancelled this compressor and the electric power requirement is reduced.The LNG composition of setting in the method shown in Figure 8 is described identical at Fig. 1 to 6 with Fig. 7 and front with condition.Therefore, Fig. 8 method of the present invention can contrast with other embodiment of the present invention shown in process and Fig. 3 to 6 is arranged earlier shown in embodiment of the present invention shown in Fig. 7, Fig. 1 and 2.
In the simulation process of Fig. 8 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters absorption tower 21 then.The logistics 41a that discharges from this pump is the overhead vapours (logistics 50) by making-90 [68 ℃] overhead vapours (distillating logistics 48) of discharging, 20 [7 ℃] of discharging in fractionation stripper 24 in contact separation device absorptive tower 21 and be heated to-101 [74 ℃] from 190 [88 ℃] product liquids (logistics 51) cooling of fractionation stripper 21 heat exchanger 12 and 13 earlier.
The liquid stream 41c of part heating uses the further heating (logistics 41d) to-54 [48 ℃] of low-lying level public work heat in heat exchanger 14 then.The operating pressure (about 465psia[3,206kPa (a)]) that is expanded to absorption tower 21 by expansion valve 20 afterwards, logistics 41e is at-58 [50 ℃] inflow tower underfeed point down.The liquid part (if any) of expansion logistics 41e is mixed with the liquid that 21 tops from the absorption tower fall, and mixed liquor stream 49 is discharged from 21 bottoms, contact arrangement absorption tower under-61 °F [52 ℃].The gas phase of expansion logistics 41e part 21 rises and contacts condensation and absorb C with the cold liquid that falls through the absorption tower
3Component reaches more heavy hydrocarbon component.
Be expanded to the operating pressure (430psia[2 of a little higher than stripper 24 by expansion valve 22 flash distillations from the mixed liquor stream 49 of 21 bottoms, absorption tower, 965kPa (a)]), make logistics 49 be cooled to-64 °F [53 ℃] (logistics 49a), enter fractionation stripper 24 at the cat head feed points then.In stripper 24, the steam stripping from logistics 49a that produces in the reboiler 25 goes out methane and C
2Component is 0.020: 1 with the mol ratio that satisfies ethane and propane.Discharge gained liquid product stream 51 bottom from stripper 24 under 190 [88 ℃], is cooled to 0 °F [18 ℃] (logistics 51a) as previously described in heat exchanger 13, flows into storage tank or further processing then.
Under 20 °F [7 ℃], leave this tower and inflow heat exchanger 12 is cooled to-98 °F [72 ℃] as previously described therein from the overhead vapours (logistics 50) of stripper 24, make the whole condensations of this logistics.Condensate stream 50a enters cat head air pump 33 then, make the pressure of logistics 50b rise to the operating pressure on a little higher than absorption tower 21, this moment, it entered heat exchanger 12 again by provide the part of whole cooling tasks to be heated to-70 [57 ℃] (logistics 50c) and part vaporization in this heat exchanger.Be expanded to by control valve 35 after the operating pressure on absorption tower 21, logistics 50d infeeds absorption tower 21 at tower middle part feed points under-75 °F [60 ℃], the liquid that falls with 21 tops from the absorption tower mixes to being used for the steam that 21 bottoms rise from the absorption tower and captures C therein
3Reach more a part of liquid of heavy ends.
Cat head distillates air-flow 48 and discharges from contact arrangement absorption tower 21 under-90 °F [68 ℃], and inflow heat exchanger 12 is cooled to-132 [91 ℃] and all condensations by carrying out heat exchange with cold LNG (logistics 41a) therein as previously described.Condensate liquid (logistics 48a) is pressurized to the operating pressure (logistics 48b) on a little higher than absorption tower 21, separated into two parts (logistics 52 and 53) then by pump 31.First's (logistics 52) is the poor LNG logistics of methane rich, and it is pressurized to 1365psia[9 by pump 32,411kPa (a)] (logistics 52a) be used for follow-up vaporization and/or course of conveying.
Another part is a reflux stream 53, and it is expanded to the operating pressure on absorption tower 21 by control valve 30.The logistics 53a of Peng Zhanging infeeds absorption tower 21 as cat head cold feed (phegma) under-131 °F [91 ℃] then.This cold reflux liquid absorbs and condensation C from the steam that rises on the top on absorption tower 21
3Component reaches more heavy hydrocarbon component.
The logistics flux of method shown in Figure 8 and energy consumption gather and are shown in the following table:
Table VIII
(Fig. 8)
Logistics flux summary sheet Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
The Table VII contrast of the Table VIII of top Fig. 8 embodiment of the present invention and Fig. 7 embodiment of the present invention shows: the liquids recovery rate of Fig. 8 embodiment is basic identical.Compressor (tower overhead gas compressor 34 among Fig. 7) will be sent into contact arrangement absorption tower 21 from the overhead vapours of fractionation stripper 24 because Fig. 8 embodiment is utilized pump (cat head air pump 33 among Fig. 8), and Fig. 8 embodiment needs electric power still less.But the required high level public work of Fig. 8 embodiment heat higher (about 19% in height).Select to adopt which kind of embodiment generally to depend on the relative cost of electric power and high level public work heat and the relative cost of pump and compressor in concrete the application.
Embodiment 7
Adopt as shown in Figure 9 another embodiment of the present invention can obtain a kind ofly can under the hot low consumption condition of high level public work, keep same C
3More complicated a little the design of component recovery.In the LNG composition of setting in the method shown in Figure 9 and condition and Fig. 7 and 8 and front is described identical at Fig. 1 to 6.Therefore, Fig. 9 method of the present invention can contrast with other embodiment of the present invention shown in process and Fig. 3 to 6 is arranged earlier shown in embodiment of the present invention shown in Fig. 7 and 8, Fig. 1 and 2.
In the simulation process of Fig. 9 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters separator 15 then.The logistics 41a that discharges from this pump was heated before entering separator 15 and makes it all or part of vaporization.In embodiment illustrated in fig. 9, logistics 41a is the compression overhead gas stream 50a by the compression overhead vapours 48a that makes-70 [57 ℃], 67 [19 ℃] and be heated to-88 [66 ℃] from 161 [72 ℃] product liquids (logistics 51) cooling of fractionation stripper 24 in heat exchanger 12 and 13 earlier.The liquid stream 41c of part heating uses the further heating (logistics 41d) of low-lying level public work heat in heat exchanger 14 then.
Logistics 41d after the heating is at-16 [27 ℃] and 596psia[4,109kPa (a)] under enter separator 15, steam (logistics 46) separates with any residual liquid (logistics 47) therein.The steam of separator (logistics 46) enters work done decompressor 18, takes out mechanical energy from this part high pressure charging.Decompressor 18 makes steam expand substantially isentropically to the operating pressure (about 415psia[2,861kPa (a)]) of tower, and described work done expansion process makes expanded gas flow 46a be cooled to the temperature of-42 [41 ℃] approximately.The expanded gas flow 46a of partial condensation infeeds absorption tower 21 as charging at tower middle part feed points then.If there is any separator liquid (logistics 47), then be expanded to the operating pressure on absorption tower 21 by expansion valve 20, infeed absorption tower 21 at tower underfeed point then.In embodiment illustrated in fig. 9, logistics 41d is vaporization fully in heat exchanger 14, thus do not need separator 15 and expansion valve 20, and expansion logistics 46a infeeds absorption tower 21 at tower underfeed point feed points.Expansion logistics 46a (with expansion logistics 47a, mix with the liquid that 21 tops from the absorption tower fall, and mixed liquor stream 49 is the 21 bottoms discharge from the absorption tower under-45 °F [43 ℃] by liquid part (if any) if present).(with expansion logistics 47a, if present) gas phase part 21 rises and contacts condensation and absorb C with the cold liquid that falls through the absorption tower expansion logistics 46a
3Component reaches more heavy hydrocarbon component.
Be expanded to the operating pressure (320psia[2 of a little higher than fractionation stripper 24 by expansion valve 22 flash distillations from the mixed liquor stream 49 of contact separation device absorptive tower 21 bottoms, 206kPa (a)]), make logistics 49 be cooled to-54 °F [48 ℃] (logistics 49a), enter fractionation stripper 24 at the cat head feed points then.In stripper 24, the steam stripping from logistics 49a that produces in the reboiler 25 goes out methane and C
2Component is 0.020: 1 with the mol ratio that satisfies ethane and propane.Discharge gained liquid product stream 51 bottom from stripper 24 under 161 [72 ℃], is cooled to 0 °F [18 ℃] (logistics 51a) as previously described in heat exchanger 13, flows into storage tank or further processing then.
Under 20 °F [6 ℃], leave this tower and flow into tower overhead gas compressor 34 (by a part of driven by power of decompressor 18 generations) from the overhead vapours (logistics 50) of stripper 24, make the operating pressure on a little higher than absorption tower 21 of pressure of logistics 50a.Logistics 50a enters heat exchanger 12, is cooled to-87 °F [66 ℃] as previously described therein, makes the whole condensations of this logistics.Condensate stream 50b is expanded to the operating pressure on absorption tower 21 by control valve 35, the logistics 50c of gained-91 [68 ℃] infeeds absorption tower 21 at tower middle part feed points then, and the liquid that falls with 21 tops from the absorption tower mixes to being used for capturing the steam C that 21 bottoms rise from the absorption tower therein
3Liquid part with heavy component.
Cat head distillates air-flow 48 21 top discharge from the absorption tower under-94 [70 ℃], flows into compressor 19 (dump power that is produced by decompressor 18 drives), is compressed into 508psia[3 therein, 501kPa (a)] (logistics 48a).Under this pressure, whole condensations when this logistics is cooled to-126 [88 ℃] as previously described in heat exchanger 12.Condensate liquid (logistics 48b) separated into two parts (logistics 52 and 53) then.First's (logistics 52) is the poor LNG logistics of methane rich, and it is pressurized to 1365psia[9 by pump 32,411kPa (a)] (logistics 52a) be used for follow-up vaporization and/or course of conveying.
Another part is a reflux stream 53, and it is expanded to the operating pressure on absorption tower 21 by control valve 30.The logistics 53a of Peng Zhanging infeeds absorption tower 21 as cat head cold feed (phegma) under-136 °F [93 ℃] then.This cold reflux liquid absorbs and condensation C from the steam that rises in the upper rectifying section on absorption tower 21
3Component reaches more heavy hydrocarbon component.
The logistics flux of method shown in Figure 9 and energy consumption gather and are shown in the following table:
Table I X
(Fig. 9)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
The Table VII of the Table I X of top Fig. 9 embodiment of the present invention and Fig. 7 of the present invention and 8 embodiments and VIII contrast show: the liquids recovery rate of Fig. 9 embodiment is basic identical.The electric power requirement of Fig. 9 embodiment is than Fig. 7 embodiment low about 3% and than Fig. 8 embodiment high about 2%.But the required high level public work of Fig. 9 embodiment of the present invention heat is starkly lower than Fig. 7 embodiment (low about 21%) or Fig. 8 embodiment (low about 34%).Select to adopt which kind of embodiment generally to depend on the relative cost of electric power and high level public work heat and the relative cost of pump and heat exchanger and compressor and decompressor in concrete the application.
Embodiment 8
Adopt another embodiment of the present invention as shown in figure 10 can obtain a kind of energy maintenance C identical with Fig. 9 embodiment
3The simpler a little embodiment of the present invention of component recovery.Among the LNG composition of setting in the method shown in Figure 10 and condition and Fig. 7 to 9 and front is described identical at Fig. 1 to 6.Therefore, Figure 10 method of the present invention can contrast with other embodiment of the present invention shown in process and Fig. 3 to 6 that has earlier shown in the embodiment of the present invention shown in Fig. 7 to 9, Fig. 1 and 2.
In the simulation process of Figure 10 method, under-255 °F [159 ℃], enter pump 11 from the pending LNG (logistics 41) of LNG jar 10.Pump 11 is increased to the pressure of LNG to be enough to make it can flow through heat exchanger and enters separator 15 then.The logistics 41a that discharges from this pump was heated before entering separator 15 and makes it all or part of vaporization.In embodiment illustrated in fig. 10, logistics 41a is the overhead gas stream 50 by the compression overhead gas stream 48a that makes-61 [52 ℃], 40 [4 ℃] and be heated to-83 [64 ℃] from 190 [88 ℃] product liquids (logistics 51) cooling of fractionation stripper 24 in heat exchanger 12 and 13 earlier.The liquid stream 41c of part heating uses the further heating (logistics 41d) of low-lying level public work heat in heat exchanger 14 then.
Logistics 41d after the heating is at-16 [26 ℃] and 621psia[4,282kPa (a)] under enter separator 15, steam (logistics 46) separates with any residual liquid (logistics 47) therein.The steam of separator (logistics 46) enters work done decompressor 18, takes out mechanical energy from this part high pressure charging.Decompressor 18 makes steam expand substantially isentropically to the operating pressure (about 380psia[2,620kPa (a)]) of tower, and described work done expansion process makes expanded gas flow 46a be cooled to the temperature of-50 [46 ℃] approximately.The expanded gas flow 46a of partial condensation infeeds absorption tower 21 at tower middle part feed points as charging then.If there is any separator liquid (logistics 47), then be expanded to the operating pressure on absorption tower 21 by expansion valve 20, infeed absorption tower 21 at tower underfeed point then.In embodiment illustrated in fig. 10, logistics 41d is vaporization fully in heat exchanger 14, thus do not need separator 15 and expansion valve 20, and expansion logistics 46a infeeds absorption tower 21 at tower underfeed point feed points.Expansion logistics 46a (with expansion logistics 47a, mix with the liquid that 21 tops from the absorption tower fall, and mixed liquor stream 49 is the 21 bottoms discharge from the absorption tower under-53 °F [47 ℃] by liquid part (if any) if present).(with expansion logistics 47a, gas phase part if present) rises by absorption tower 21 and contacts condensation and absorb C with the cold liquid that falls expansion logistics 46a
3Component reaches more heavy hydrocarbon component.
Enter pump 23 and be pumped to the operating pressure (430psia[2,965kPa (a)]) of a little higher than stripper 24 from the mixed liquor of contact separation device absorptive tower 21 bottoms stream 49.Gained logistics 49a enters fractionation stripper 24 at the cat head feed points under-52 °F [47 ℃] then.In stripper 24, the steam stripping from logistics 49a that produces in the reboiler 25 goes out methane and C
2Component is 0.020: 1 with the mol ratio that satisfies ethane and propane.Discharge gained liquid product stream 51 bottom from stripper 24 under 190 [88 ℃], is cooled to 0 °F [18 ℃] (logistics 51a) as previously described in heat exchanger 13, flows into storage tank or further processing then.
Under 40 °F [4 ℃], leave this tower and enter heat exchanger 12 from the overhead vapours (logistics 50) of stripper 24, be cooled to therein as previously described-89 °F [67 ℃], make the whole condensations of this logistics.Condensate stream 50a is expanded to the operating pressure on absorption tower 21 by control valve 35, the logistics 50b of gained-94 [70 ℃] infeeds absorption tower 21 at tower middle part feed points then, and the liquid that falls with 21 tops from the absorption tower mixes to being used for the steam that 21 bottoms rise from the absorption tower and captures C therein
3Reach more a part of liquid of heavy ends.
Another part is a reflux stream 53, and it is expanded to the operating pressure on absorption tower 21 by control valve 30.The logistics 53a of Peng Zhanging infeeds absorption tower 21 as cat head cold feed (phegma) under-141 °F [96 ℃] then.This cold reflux liquid absorbs and condensation C from the steam that rises in the upper rectifying section on absorption tower 21
3Component reaches more heavy hydrocarbon component.
The logistics flux of method shown in Figure 10 and energy consumption gather and are shown in the following table:
Table X
(Figure 10)
Logistics flux one cable table Lb.Moles/Hr[kg moles/Hr]
* (based on the flow that does not round up)
The Table VII of the Table X of top Figure 10 embodiment of the present invention and Fig. 7 to 9 embodiment of the present invention to IX contrast shows: the liquids recovery rate of Figure 10 embodiment is basic identical.The electric power requirement of Figure 10 embodiment is than Fig. 7 embodiment low about 1% and than Fig. 8 and 9 embodiments difference high about 4% and 2%.The required high level public work of Figure 10 embodiment of the present invention heat is starkly lower than Fig. 7 and 8 embodiments (hanging down about 7% and 22% respectively), but than Fig. 9 embodiment high about 18%.Select to adopt which kind of embodiment generally to depend on the relative cost of electric power and high level public work heat and the counter investment expense of pump, heat exchanger, compressor and decompressor in concrete the application.
Other embodiment
May be more suitable under some situation making reflux stream 53 cold excessively, rather than utilize the cold LNG logistics that enters heat exchanger 12 with another process-stream.In the case, can adopt alternative embodiment of the present invention shown in Figure 11 to 13.In Figure 11 and 12 embodiments, a part (logistics 42) of leaving the part heating LNG logistics 41b of heat exchanger 12 is expanded to the operating pressure of a little higher than fractionating column 21 (Figure 11) or absorption tower 21 (Figure 12) by expansion valve 17, logistics 42a after the expansion enters heat exchanger 29 and is heated, and makes reflux stream 53 cold excessively simultaneously.Cross cold reflux stream 53a then and be expanded to the operating pressure of fractionating column 21 (Figure 11) or contact separation device absorptive tower 21 (Figure 12) by expansion valve 30, the logistics 53b after the expansion infeeds fractionating column 21 (Figure 11) or absorption tower 21 (Figure 12) as cat head cold feed (phegma).The heated stream 42b that leaves heat exchanger 29 infeeds this tower at tower middle part feed points, as adding reflux stream.Perhaps, shown in dotted line in Figure 11 and 12, before entering heat exchanger 12, from LNG logistics 41a, take out logistics 42.In the embodiment of Figure 13, by make logistics 50b be expanded to the operating pressure on a little higher than absorption tower 21 with control valve 17 and will expand after logistics 50c introducing heat exchanger 29 make that 50 condensations of fractionation stripper 24 overhead gas stream are produced to add reflux stream cold excessively with reflux stream 53 in heat exchanger 29.Heated stream 50d infeeds this tower at tower middle part feed points then.
Whether decision reflux stream 53 is expanded to made it cold many factors that depend on before the tower operating pressure, comprised that LNG forms, the desired rate of recovery etc.Shown in dotted line among Fig. 3 to 10, if wanted cold then heat exchanger 12 is sent in logistics 53, if perhaps do not want cold then directly send into expansion valve 30.Whether similarly, add reflux stream 42 is expanded to and will heats and must assess at every kind of application before the tower operating pressure.Shown in dotted line among Fig. 3,6 and 13, if do not think heating then can before heating LNG logistics 41a, take out logistics 42 and directly send into expansion valve 17, if perhaps want to heat then from the LNG logistics 41b of part heating, take out logistics 42 and send into expansion valve 17.On the other hand, heating and the part vaporization of adding reflux stream 50b as shown in Figure 8 may be unfavorable, because this makes and enters absorption tower 21 and be used for the steam that 21 bottoms rise from the absorption tower and capture C
2Component and/or C
3Component and the more amount of liquid minimizing of heavy hydrocarbon component.And as shown in phantom in Figure 8, logistics 50b can directly send into expansion valve 35 and enter absorption tower 21 then.
When pending LNG is poor or attempt when in heat exchanger 12,13 and 14 LNG being vaporized fully, the separator 15 among Fig. 3 to 5 and 9 to 11 may be not too appropriate.According to the pressure that feed pump 11 is left in the amount and the LNG logistics of heavy hydrocarbon in the LNG charging, the hot LNG logistics of leaving heat exchanger 14 may not contain any liquid (because be higher than its dew point, perhaps because be higher than its critical condensation pressure).In the case, then by leaving out separator 15 and expansion valve 20 shown in the dotted line.
In the embodiment shown, logistics 48a among Fig. 3,5 and 9 to 11, logistics 48b among Fig. 4, logistics 48 among Fig. 6 to 8,12 and 13, the whole condensations of logistics 50a in logistics 50 and Fig. 7 and 9 among Fig. 6,8,10,12 and 13.Agree with under some situation making one of these logistics or two cold excessively, and agree with only partial condensation under other situations.If adopt one of logistics or the method for two partial condensations, then may need to handle uncooled steam, with compressor or miscellaneous equipment steam pressure is raise and makes it to add the condensate liquid that is pumped.Perhaps, uncooled steam is sent into fuel system or other this type of application of this equipment.
The condition of LNG, instrument size, available devices or other factors can demonstrate the work done decompressor 18 of leaving out in Fig. 3 to 5 and 9 to 11 or substitute with alternative bloating plant (as expansion valve) is feasible.Although describe the expansion process of each logistics, under situation about being fit to, can adopt other bloating plant with specific bloating plant.
Should also be noted that expansion valve 17,20,22,30 and/or 35 can use decompressor (turbo-expander) to replace, thereby from the step-down of following logistics, extract logistics 42 among merit: Fig. 3,6 and 11 to 13; Logistics 45a among Fig. 4; Logistics 47 among Fig. 3 to 5 and 9 to 11; Logistics 43b among Fig. 6,12 and 13; Logistics 41d among Fig. 7 and 8; Logistics 49 among Fig. 6 to 9,12 and 13; Logistics 53a among Fig. 3 to 5 and 11 to 13; Logistics 53 among Fig. 6 to 10; Logistics 50b among Fig. 6,7,9,12 and 13; Logistics 50c among Fig. 8; And/or logistics 50a among Figure 10.Under these situations, may need to make LNG (logistics 41) and/or other liquid stream is pressurized to elevated pressures so that the extraction of merit is feasible with pump.This merit can be used for providing power for pumping LNG incoming flow, the poor LNG product stream of pumping, compression overhead gas stream or generating.Selecting to use valve still is the concrete condition that decompressor depends on the LNG processing target.
Among Fig. 3 to 13, each heat exchanger that is used for the great majority application has been shown.But also can with two or more heat exchange action be incorporated into common heat exchanger, as the heat exchanger among Fig. 3 to 13 12,13 and 14 is merged into common heat exchanger.May be beneficial under some situation heat exchange action is divided into a plurality of heat exchangers.Using shown in the decision is to merge heat exchange action or adopt a plurality of heat exchangers to depend on many factors, includes but not limited to LNG flow, heat exchanger size, stream temperature etc.
The relative quantity that will be appreciated that charging in each the LNG charging branch that infeeds fractionating column 21 or absorption tower 21 depends on many factors, comprises LNG composition, the heat that can extract from charging economically and the amount of available power.How the charging that infeeds cat head can improve the rate of recovery, and the load of reboiler 25 is increased, thereby the requirement of high level public work heat is increased.The increase of tower underfeed amount reduces the consumption of high level public work heat but the product rate of recovery is descended.The relative position of tower middle part charging can according to LNG form or all as expected the rate of recovery and feed stream heating process in generate steam other factorses such as amount change.In addition, can two or more feed stream or its part be merged, will merge logistics then and infeed tower middle part feed entrance point according to the relative temperature and the amount of each logistics.
Fig. 3 to 6 embodiment is given among the embodiment, has illustrated C
2The component and the removal process of heavy hydrocarbon component more, and Fig. 7 to 10 embodiment is given and has been illustrated C among the embodiment
3Component reaches the more removal process of heavy hydrocarbon component.But it is believed that and only want to reclaim C
3Component and more during the heavy hydrocarbon component embodiment of Fig. 3 to 6 also be favourable, and want to reclaim C
2Component and more during the heavy hydrocarbon component Fig. 7 to 10 embodiment also be favourable.Similarly, believe that Figure 11 to 13 embodiment is used to reclaim C
2Component and heavy hydrocarbon component and be used to reclaim C more
3Component reaches more, and the heavy hydrocarbon component all is favourable.
The invention provides the C that the per unit public work consumption that needs in the technological operation is reached
2Component reaches more heavy hydrocarbon component or C
3Component and the method that is improved of heavy hydrocarbon component recovery more.The improvements of the public work consumption that needs in technological operation can reduce from the compression or the electric power amount of pumping needs, find out the energy minimizing of tower reboiler needs or its combining form.Perhaps, advantage of the present invention may be embodied in the public work consumption of specified rate and realizes the higher rate of recovery or the rate of recovery is higher consumes improved certain combination with public work.
Although to it is believed that the situation for the preferred embodiment of the invention is described, those skilled in the art will recognize that and under the situation that does not deviate from the spirit of the present invention that limits as following claims, to carry out other modification, for example make the present invention be suitable for various conditions, type of feed or other requirement it
Claims (67)
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is divided at least first logistics and second logistics;(b) make described first logistics be expanded to lower pressure, infeed fractionating column at first tower middle part feed entrance point then;(c) described second logistics is heated to is enough to make it part vaporization, thereby form air-flow and liquid stream;(d) make described flow expansion infeed described fractionating column to described lower pressure and at second tower first feed entrance point;(e) make described liquid stream be expanded to described lower pressure and infeed described fractionating column at second tower second feed entrance point;(f) the upper area discharge from described fractionating column distillates air-flow and compression;(g) thus make the air-flow that distillates of described compression be cooled to and be enough to make it at least partial condensation and form condensate flow, described cooling procedure is at least described second logistics a part of described heat effect is provided;(h) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(i) described reflux stream is infeeded described fractionating column at the cat head feed entrance point; With(j) temperature of the described charging of the amount of described reflux stream and temperature and described fractionating column can effectively make the tower top temperature of described fractionating column remain on uniform temperature, thereby reclaims most described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) with described liquefied natural gas heating, be divided into first logistics and second logistics then at least;(b) make described first logistics be expanded to lower pressure, infeed fractionating column at first tower middle part feed entrance point then;(c) described second logistics is heated to is enough to make it part vaporization, thereby form air-flow and liquid stream;(d) make described flow expansion infeed described fractionating column to described lower pressure and at second tower first feed entrance point;(e) make described liquid stream be expanded to described lower pressure and infeed described fractionating column at second tower second feed entrance point;(f) the upper area discharge from described fractionating column distillates air-flow and compression;(g) thus make the air-flow that distillates of described compression be cooled to and be enough to make it at least partial condensation and form condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(h) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(i) described reflux stream is infeeded described fractionating column at the cat head feed entrance point; With(j) temperature of the described charging of the amount of described reflux stream and temperature and described fractionating column can make the tower top temperature of described fractionating column remain on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is divided at least first logistics and second logistics;(b) make described first logistics be expanded to lower pressure, infeed fractionating column at first tower middle part feed entrance point then;(c) described second logistics is heated to is enough to make it vaporization, thereby form air-flow;(d) make described flow expansion infeed described fractionating column to described lower pressure and at second tower middle part feed entrance point;(e) the upper area discharge from described fractionating column distillates air-flow and compression;(f) thus make the air-flow that distillates of described compression be cooled to and be enough to make it at least partial condensation and form condensate flow, described cooling procedure is at least described second logistics a part of described heat effect is provided;(g) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(h) described reflux stream is infeeded described fractionating column at the cat head feed entrance point; With(i) temperature of the described charging of the amount of described reflux stream and temperature and described fractionating column can make the tower top temperature of described fractionating column remain on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) with described liquefied natural gas heating, be divided into first logistics and second logistics then at least;(b) make described first logistics be expanded to lower pressure, infeed fractionating column at first tower middle part feed entrance point then;(c) described second logistics is heated to is enough to make it vaporization, thereby form air-flow;(d) make described flow expansion infeed described fractionating column to described lower pressure and at second tower middle part feed entrance point;(e) the upper area discharge from described fractionating column distillates air-flow and compression;(f) thus make the air-flow that distillates of described compression be cooled to and be enough to make it at least partial condensation and form condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(g) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(h) described reflux stream is infeeded described fractionating column at the cat head feed entrance point; With(i) temperature of the described charging of the amount of described reflux stream and temperature and described fractionating column can make the tower top temperature of described fractionating column remain on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to make it part vaporization, thereby form air-flow and liquid stream;(b) described air-flow is divided at least first logistics and second logistics;(c) make described first logistics be cooled to its all condensation basically, thereby be expanded to further cooling of lower pressure then;(d) first logistics with described expansion cooling infeeds fractionating column at first tower middle part feed entrance point;(e) make described second logistics be expanded to described lower pressure and infeed described fractionating column at second tower first feed entrance point;(f) make described liquid stream be expanded to described lower pressure and infeed described fractionating column at second tower second feed entrance point;(g) the upper area discharge from described fractionating column distillates air-flow and heating, and described heating process is at least described first logistics a part of described cooling effect is provided;(h) air-flow that distillates after the described heating is compressed;(i) thus make the air-flow that distillates of described compression heating be cooled to and be enough to make it at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(j) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(k) described reflux stream is infeeded described fractionating column at the cat head feed entrance point; With(l) temperature of the described charging of the amount of described reflux stream and temperature and described fractionating column can make the tower top temperature of described fractionating column remain on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to make it vaporization, thereby form air-flow;(b) described air-flow is divided at least first logistics and second logistics;(c) make described first logistics be cooled to all condensations basically, thereby be expanded to further cooling of lower pressure then;(d) first logistics with described expansion cooling infeeds fractionating column at first tower middle part feed entrance point;(e) make described second logistics be expanded to described lower pressure and infeed described fractionating column at second tower middle part feed entrance point;(f) the upper area discharge from described fractionating column distillates air-flow and heating, and described heating process is at least described first logistics a part of described cooling effect is provided;(g) air-flow that distillates after the described heating is compressed;(h) thus make the air-flow that distillates of described compression heating be cooled to and be enough to make it at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(i) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(j) described reflux stream is infeeded described fractionating column at the cat head feed entrance point; With(k) temperature of the described charging of the amount of described reflux stream and temperature and described fractionating column can make the tower top temperature of described fractionating column remain on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to make it part vaporization, thereby form air-flow and liquid stream;(b) make described flow expansion infeed described fractionating column to lower pressure and at first tower middle part feed entrance point;(c) make described liquid stream be expanded to described lower pressure and infeed described fractionating column at second tower middle part feed entrance point;(d) the upper area discharge from described fractionating column distillates air-flow and compression;(e) thus make the air-flow that distillates of described compression be cooled to and be enough to make it at least partial condensation and form condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(f) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(g) described reflux stream is infeeded described fractionating column at the cat head feed entrance point; With(h) temperature of the described charging of the amount of described reflux stream and temperature and described fractionating column can make the tower top temperature of described fractionating column remain on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to make it vaporization, thereby form air-flow;(b) make described flow expansion infeed described fractionating column to lower pressure and at tower middle part feed entrance point;(c) the upper area discharge from described fractionating column distillates air-flow and compression;(d) thus make the air-flow that distillates of described compression be cooled to and be enough to make it at least partial condensation and form condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(e) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(f) described reflux stream is infeeded described fractionating column at the cat head feed entrance point; With(g) temperature of the described charging of the amount of described reflux stream and temperature and described fractionating column can make the tower top temperature of described fractionating column remain on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is divided at least first logistics and second logistics;(b) make described first logistics be expanded to lower pressure, infeed the absorption tower at first tower middle part feed entrance point then, liquid stream at the bottom of generation overhead gas stream and the tower;(c) described second logistics is heated to is enough to make it part vaporization;(d) make second logistics of described heating be expanded to described lower pressure and infeed described absorption tower in the underfeed position;(e) liquid stream at the bottom of the described tower is infeeded the fractionation stripper at the cat head feed entrance point;(f) the upper area discharge from described fractionation stripper distillates air-flow and is cooled to all condensations basically, and described cooling procedure is at least described second logistics a part of described heat effect is provided;(g), infeed described absorption tower at second tower middle part feed entrance point then with the logistics of described basic condensation pump supercharging;(h) thus described overhead gas stream is cooled to be enough at least that partial condensation forms condensate flow, described cooling procedure is at least described second logistics a part of described heat effect is provided;(i), be divided into described volatile liquid cut and the reflux stream that comprises most of described methane then at least with the pump supercharging of described condensate flow;(j) described reflux stream is infeeded described absorption tower at the cat head feed entrance point; With(k) amount of described reflux stream and temperature and infeed described absorption tower and the temperature of the described charging of described fractionation stripper can make the tower top temperature of described absorption tower and described fractionation stripper remain on uniform temperature, thus most of described more heavy hydrocarbon component in described low volatility liquid distillate, reclaimed by fractionation.
- One kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) with described liquefied natural gas heating, be divided into first logistics and second logistics then at least;(b) make described first logistics be expanded to lower pressure, infeed the absorption tower at first tower middle part feed entrance point then, liquid stream at the bottom of generation overhead gas stream and the tower;(c) described second logistics is heated to is enough to make it part vaporization;(d) make second logistics of described heating be expanded to described lower pressure and infeed described absorption tower in the underfeed position;(e) liquid stream at the bottom of the described tower is infeeded the fractionation stripper at the cat head feed entrance point;(f) the upper area discharge from described fractionation stripper distillates air-flow and is cooled to all condensations basically, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(g), infeed described absorption tower at second tower middle part feed entrance point then with the logistics of described basic condensation pump supercharging;(h) thus described overhead gas stream is cooled to be enough at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(i), be divided into described volatile liquid cut and the reflux stream that comprises most of described methane then at least with the pump supercharging of described condensate flow;(j) described reflux stream is infeeded described absorption tower at the cat head feed entrance point; With(k) amount of described reflux stream and temperature and infeed described absorption tower and the temperature of the described charging of described fractionation stripper can make the tower top temperature of described absorption tower and described fractionation stripper remain on uniform temperature, thus most of described more heavy hydrocarbon component in described low volatility liquid distillate, reclaimed by fractionation.
- 11. one kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to make it to vaporize to small part;(b) make the liquefied natural gas after the described heating be expanded to lower pressure, infeed the absorption tower in the underfeed position then, produce liquid stream at the bottom of overhead gas stream and the tower;(c) liquid stream at the bottom of the described tower is infeeded the fractionation stripper at the cat head feed entrance point;(d) the upper area discharge from described fractionation stripper distillates air-flow and compression;(e) make the air-flow that distillates of described compression be cooled to and be enough to partial condensation at least, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(f) the compression logistics of described cooling infeeds described absorption tower at tower middle part feed entrance point;(g) thus described overhead gas stream is cooled to be enough at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(h), be divided into described volatile liquid cut and the reflux stream that comprises most of described methane then at least with the pump supercharging of described condensate flow;(i) described reflux stream is infeeded described absorption tower at the cat head feed entrance point; With(j) amount of described reflux stream and temperature and infeed described absorption tower and the temperature of the described charging of described fractionation stripper can make the tower top temperature of described absorption tower and described fractionation stripper remain on uniform temperature, thus most of described more heavy hydrocarbon component in described low volatility liquid distillate, reclaimed by fractionation.
- 12. one kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to vaporize to small part;(b) make the liquefied natural gas after the described heating be expanded to lower pressure, infeed the absorption tower in the underfeed position then, produce liquid stream at the bottom of overhead gas stream and the tower;(c) liquid stream at the bottom of the described tower is infeeded the fractionation stripper at the cat head feed entrance point;(d) the upper area discharge from described fractionation stripper distillates air-flow and is cooled to basic all condensations, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(e) logistics of described basic condensation pump supercharging infeeds described absorption tower at tower middle part feed entrance point then;(f) thus described overhead gas stream is cooled to be enough at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(g), be divided into described volatile liquid cut and the reflux stream that comprises most of described methane then at least with the pump supercharging of described condensate flow;(h) described reflux stream is infeeded described absorption tower at the cat head feed entrance point; With(i) amount of described reflux stream and temperature and infeed described absorption tower and the temperature of the described charging of described fractionation stripper can make the tower top temperature of described absorption tower and described fractionation stripper remain on uniform temperature, thus most of described more heavy hydrocarbon component in described low volatility liquid distillate, reclaimed by fractionation.
- 13. one kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to, thereby form air-flow and liquid stream to small part vaporization;(b) make described flow expansion to lower pressure, infeed the absorption tower in the first underfeed position then, liquid stream at the bottom of generation overhead gas stream and the tower;(c) make described liquid stream be expanded to described lower pressure and infeed described absorption tower in the second underfeed position;(d) liquid stream at the bottom of the described tower is infeeded the fractionation stripper at the cat head feed entrance point;(e) the upper area discharge from described fractionation stripper distillates air-flow and compression;(f) make the air-flow that distillates of described compression be cooled to and be enough to partial condensation at least, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(g) the compression logistics of described cooling infeeds described absorption tower at tower middle part feed entrance point;(h) with described overhead gas stream compression;(i) thus the overhead gas stream of described compression is cooled to be enough at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(j) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(k) described reflux stream is infeeded described absorption tower at the cat head feed entrance point; With(l) amount of described reflux stream and temperature and infeed described absorption tower and the temperature of the described charging of described fractionation stripper can make the tower top temperature of described absorption tower and described fractionation stripper remain on uniform temperature, thus most of described more heavy hydrocarbon component in described low volatility liquid distillate, reclaimed by fractionation.
- 14. one kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to vaporize to small part;(b) make the liquefied natural gas after the described heating be expanded to lower pressure, infeed the absorption tower in the underfeed position then, produce liquid stream at the bottom of overhead gas stream and the tower;(c) liquid stream at the bottom of the described tower is infeeded the fractionation stripper at the cat head feed entrance point;(d) the upper area discharge from described fractionation stripper distillates air-flow and compression;(e) make the air-flow that distillates of described compression be cooled to and be enough to partial condensation at least, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(f) the compression logistics of described cooling infeeds described absorption tower at tower middle part feed entrance point;(g) with described overhead gas stream compression;(h) thus the overhead gas stream of described compression is cooled to be enough at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(i) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(j) described reflux stream is infeeded described absorption tower at the cat head feed entrance point; With(k) amount of described reflux stream and temperature and infeed described absorption tower and the temperature of the described charging of described fractionation stripper can make the tower top temperature of described absorption tower and described fractionation stripper remain on uniform temperature, thus most of described more heavy hydrocarbon component in described low volatility liquid distillate, reclaimed by fractionation.
- 15. one kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to, thereby form air-flow and liquid stream to small part vaporization;(b) make described flow expansion to lower pressure, infeed the absorption tower in the first underfeed position then, liquid stream at the bottom of generation overhead gas stream and the tower;(c) make described liquid stream be expanded to described lower pressure and infeed described absorption tower in the second underfeed position;(d) liquid stream at the bottom of the described tower is used the pump supercharging, infeed the fractionation stripper at the cat head feed entrance point then;(e) discharge to distillate air-flow and be cooled to from the upper area of described fractionation stripper and be enough to partial condensation at least, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(f) logistics that distillates of described cooling infeeds described absorption tower at tower middle part feed entrance point;(g) with described overhead gas stream compression;(h) thus the overhead gas stream of described compression is cooled to be enough at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(i) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(j) described reflux stream is infeeded described absorption tower at the cat head feed entrance point; With(k) amount of described reflux stream and temperature and infeed described absorption tower and the temperature of the described charging of described fractionation stripper can make the tower top temperature of described absorption tower and described fractionation stripper remain on uniform temperature, thus most of described more heavy hydrocarbon component in described low volatility liquid distillate, reclaimed by fractionation.
- 16. one kind will comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the method for the low volatility liquid distillate of most of described more heavy hydrocarbon component, wherein(a) described liquefied natural gas is heated to is enough to vaporize to small part;(b) make the liquefied natural gas after the described heating be expanded to lower pressure, infeed the absorption tower in the underfeed position then, produce liquid stream at the bottom of overhead gas stream and the tower;(c) liquid stream at the bottom of the described tower is used the pump supercharging, infeed the fractionation stripper at the cat head feed entrance point then;(d) discharge to distillate air-flow and be cooled to from the upper area of described fractionation stripper and be enough to partial condensation at least, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(e) logistics that distillates of described cooling infeeds described absorption tower at tower middle part feed entrance point;(f) with described overhead gas stream compression;(g) thus the overhead gas stream of described compression is cooled to be enough at least that partial condensation forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(h) described condensate flow is divided at least described volatile liquid cut and the reflux stream that comprises most of described methane;(i) described reflux stream is infeeded described absorption tower at the cat head feed entrance point; With(j) amount of described reflux stream and temperature and infeed described absorption tower and the temperature of the described charging of described fractionation stripper can make the tower top temperature of described absorption tower and described fractionation stripper remain on uniform temperature, thus most of described more heavy hydrocarbon component in described low volatility liquid distillate, reclaimed by fractionation.
- 17. the method for claim 1 or 3, wherein said reflux stream is further cooled, and infeeds described fractionating column at described cat head feed entrance point then, and described cooling procedure is at least described second logistics a part of described heat effect is provided.
- 18. claim 2,4,5,6,7 or 8 method, wherein said reflux stream is further cooled, and infeeds described fractionating column at described cat head feed entrance point then, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 19. the method for claim 9, wherein said reflux stream is further cooled, and infeeds described absorption tower at described cat head feed entrance point then, and described cooling procedure is at least described second logistics a part of described heat effect is provided.
- 20. claim 10,11,12,13,14,15 or 16 method, wherein said reflux stream is further cooled, infeed described absorption tower at described cat head feed entrance point then, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 21. the method for claim 12, wherein the basic condensate flow of described pump supercharging to be heated, infeed described absorption tower at described tower middle part feed entrance point then, described heating process is at least and describedly distillates air-flow or described overhead gas stream provides a part of described cooling effect.
- 22. the method for claim 21, wherein said reflux stream is further cooled, and infeeds described absorption tower at described cat head feed entrance point then, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 23. claim 1,2,3 or 4 method, wherein(1) described reflux stream is further cooled off and infeed described fractionating column at described cat head feed entrance point then;(2) make described first logistics be expanded to described lower pressure and heating subsequently, described heating process is at least described reflux stream provides a part described further cooling effect; With(3) described first logistics that adds thermal expansion infeeds described fractionating column at described first tower middle part feed entrance point.
- 24. the method for claim 9 or 10, wherein(1) described reflux stream is further cooled off and infeed described absorption tower at described cat head feed entrance point then;(2) make described first logistics be expanded to described lower pressure and heat then, described heating process is at least described reflux stream provides a part described further cooling effect; With(3) described first logistics that adds thermal expansion infeeds described absorption tower at described first tower middle part feed entrance point.
- 25. the method for claim 9 or 10, wherein(1) described reflux stream is further cooled off and infeed described absorption tower at described cat head feed entrance point then;(2) logistics with described basic condensation heats then with the pump supercharging, and described heating process is at least described reflux stream provides a part described further cooling effect; With(3) described heating and infeed described absorption tower at described second tower middle part feed entrance point with the basic condensate flow of pump supercharging.
- 26. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) first shunting device receives described liquefied natural gas and it is divided into first logistics and second logistics at least;(b) first bloating plant is connected with described first part flow arrangement and receives described first logistics and to make it to be expanded to lower pressure, and described first bloating plant connects also that fractionating column connects so that first logistics of described expansion is infeeded at first tower middle part feed entrance point;(c) heat-exchange apparatus, being connected with described first shunting device to receive described second logistics and to be heated to is enough to the part vaporization;(d) separation equipment is connected second logistics that receives the vaporization of described heating rear section and makes it to be separated into air-flow and liquid stream with described heat-exchange apparatus;(e) second bloating plant is connected with described separation equipment and receives described air-flow and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described fractionating column so that supply described expanded gas flow at second tower first feed entrance point;(f) the 3rd bloating plant is connected with described separation equipment and receives described liquid stream and to make it to be expanded to described lower pressure, and described the 3rd bloating plant also is connected with described fractionating column so that supply described inflation fluid at second tower second feed entrance point and flows;(g) device for transferring is connected to discharge with the upper area of described fractionating column and distillates air-flow;(h) compression device is connected with described exhaust apparatus to receive and describedly distillates air-flow and with its compression;(i) thus described heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough at least partial condensation and forming condensate flow of described compression, described cooling procedure is at least described second logistics a part of described heat effect is provided;(j) second shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described second shunting device also is connected with described fractionating column so that supply described reflux stream at the cat head feed entrance point to described fractionating column; With(k) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 27. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus receives described liquefied natural gas and is heated;(b) first shunting device is connected the liquefied natural gas that receives after the described heating and it is divided into first logistics and second logistics at least with described heat-exchange apparatus;(c) first bloating plant is connected with described first shunting device and receives described first logistics and to make it to be expanded to lower pressure, and described first bloating plant also is connected with fractionating column so that supply first logistics of described expansion at first tower middle part feed entrance point;(d) firing equipment, being connected with described first shunting device to receive described second logistics and to be heated to is enough to the part vaporization;(e) separation equipment is connected second logistics that receives the vaporization of described heating rear section and makes it to be separated into air-flow and liquid stream with described firing equipment;(f) second bloating plant is connected with described separation equipment and receives described air-flow and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described fractionating column so that supply described expanded gas flow at second tower first feed entrance point;(g) the 3rd bloating plant is connected with described separation equipment and receives described liquid stream and to make it to be expanded to described lower pressure, and described the 3rd bloating plant also is connected with described fractionating column so that supply described inflation fluid at second tower second feed entrance point and flows;(h) device for transferring is connected to discharge with the upper area of described fractionating column and distillates air-flow;(i) compression device is connected with described device for transferring to receive and describedly distillates air-flow and with its compression;(j) thus described heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough at least partial condensation and forming condensate flow of described compression, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(k) second shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described second shunting device also is connected with described fractionating column so that supply described reflux stream at the cat head feed entrance point to described fractionating column; With(l) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 28. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) first shunting device receives described liquefied natural gas and it is divided into first logistics and second logistics at least;(b) first bloating plant is connected with described first shunting device and receives described first logistics and to make it to be expanded to lower pressure, and described first bloating plant also is connected with fractionating column so that supply first logistics of described expansion at first tower middle part feed entrance point;(c) heat-exchange apparatus is enough to vaporization and forms air-flow thereby be connected with described first shunting device to receive described second logistics and to be heated to;(d) second bloating plant is connected with described heat-exchange apparatus and receives described air-flow and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described fractionating column so that supply described expanded gas flow at second tower middle part feed entrance point;(e) device for transferring is connected to discharge with the upper area of described fractionating column and distillates air-flow;(f) compression device is connected with described device for transferring to receive and describedly distillates air-flow and with its compression;(g) thus described heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough at least partial condensation and forming condensate flow of described compression, described cooling procedure is at least described second logistics a part of described heat effect is provided;(h) second shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described second shunting device also is connected with described fractionating column so that supply described reflux stream at the cat head feed entrance point to described fractionating column; With(i) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 29. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus receives described liquefied natural gas and is heated;(b) first shunting device is connected the liquefied natural gas that receives after the described heating and it is divided into first logistics and second logistics at least with described heat-exchange apparatus;(c) first bloating plant is connected with described first shunting device and receives described first logistics and to make it to be expanded to lower pressure, and described first bloating plant also is connected with fractionating column so that supply first logistics of described expansion at first tower middle part feed entrance point;(d) firing equipment is enough to vaporization and forms air-flow thereby be connected with described first shunting device to receive described second logistics and to be heated to;(e) second bloating plant is connected with described firing equipment and receives described air-flow and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described fractionating column so that supply described expanded gas flow at second tower middle part feed entrance point;(f) device for transferring is connected to discharge with the upper area of described fractionating column and distillates air-flow;(g) compression device is connected with described device for transferring to receive and describedly distillates air-flow and with its compression;(h) thus described heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough at least partial condensation and forming condensate flow of described compression, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(i) second shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described second shunting device also is connected with described fractionating column so that supply described reflux stream at the cat head feed entrance point to described fractionating column; With(j) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 30. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) first heat-exchange apparatus, receiving described liquefied natural gas and being heated to is enough to the part vaporization;(b) separation equipment is connected the logistics that receives the vaporization of described heating rear section and it is separated into air-flow and liquid stream with described first heat-exchange apparatus;(c) first shunting device is connected with described separation equipment and receives described air-flow and it is divided into first logistics and second logistics at least;(d) second heat-exchange apparatus, being connected with described first shunting device to receive described first logistics and to make it to be cooled to is enough to basic condensation;(e) first bloating plant, be connected first logistics that receives described basic condensation with described second heat-exchange apparatus and make it to be expanded to lower pressure, described first bloating plant also is connected with fractionating column so that supply first logistics of described expansion at first tower middle part feed entrance point;(f) second bloating plant is connected with described first shunting device and receives described second logistics and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described fractionating column so that supply described expanded gas flow at second tower first feed entrance point;(g) the 3rd bloating plant is connected with described separation equipment and receives described liquid stream and to make it to be expanded to described lower pressure, and described the 3rd bloating plant also is connected with described fractionating column so that supply described inflation fluid at second tower second feed entrance point and flows;(h) device for transferring is connected to discharge with the upper area of described fractionating column and distillates air-flow;(i) described second heat-exchange apparatus also is connected with described device for transferring to receive and describedly distillates air-flow and be heated, and described heating process is at least described first logistics a part of described cooling effect is provided;(j) compression device, be connected with described second heat-exchange apparatus receive after the described heating distillate air-flow and with its compression;(k) thus described first heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough at least that partial condensation forms condensate flow of described compression heating, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(l) second shunting device, be connected with described first heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described second shunting device also is connected with described fractionating column so that supply described reflux stream at the cat head feed entrance point to described fractionating column; With(m) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 31. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) first heat-exchange apparatus is enough to vaporization formation air-flow thereby receive described liquefied natural gas and be heated to;(b) first shunting device is connected with described first heat-exchange apparatus and receives described air-flow and it is divided into first logistics and second logistics at least;(c) second heat-exchange apparatus, being connected with described first shunting device to receive described first logistics and to make it to be cooled to is enough to basic condensation;(d) first bloating plant, be connected first logistics that receives described basic condensation with described second heat-exchange apparatus and make it to be expanded to lower pressure, described first bloating plant also is connected with fractionating column so that supply first logistics of described expansion at first tower middle part feed entrance point;(e) second bloating plant is connected with described first shunting device and receives described second logistics and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described fractionating column so that supply described expanded gas flow at second tower middle part feed entrance point;(f) device for transferring is connected to discharge with the upper area of described fractionating column and distillates air-flow;(g) described second heat-exchange apparatus also is connected with described device for transferring to receive and describedly distillates air-flow and be heated, and described heating process is at least described first logistics a part of described cooling effect is provided;(h) compression device, be connected with described second heat-exchange apparatus receive after the described heating distillate air-flow and with its compression;(i) thus described first heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough at least that partial condensation forms condensate flow of described compression heating, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(j) second shunting device, be connected with described first heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described second shunting device also is connected with described fractionating column so that supply described reflux stream at the cat head feed entrance point to described fractionating column; With(k) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 32. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus, receiving described liquefied natural gas and being heated to is enough to the part vaporization;(b) separation equipment is connected the logistics that receives the vaporization of described heating rear section and it is separated into air-flow and liquid stream with described heat-exchange apparatus;(c) first bloating plant is connected with described separation equipment and receives described air-flow and to make it to be expanded to lower pressure, and described first bloating plant also is connected with fractionating column to come at first tower middle part feed entrance point supplies described expanded gas flow;(d) second bloating plant is connected with described separation equipment and receives described liquid stream and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described fractionating column so that supply described inflation fluid at second tower middle part feed entrance point and flows;(e) device for transferring is connected to discharge with the upper area of described fractionating column and distillates air-flow;(f) compression device is connected with described device for transferring to receive and describedly distillates air-flow and with its compression;(g) thus described heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough at least partial condensation and forming condensate flow of described compression, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(h) shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described shunting device also is connected with described fractionating column so that supply described reflux stream at the cat head feed entrance point to described fractionating column; With(i) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 33. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus is enough to vaporization formation air-flow thereby receive described liquefied natural gas and be heated to;(b) bloating plant is connected with described heat-exchange apparatus and receives described air-flow and to make it to be expanded to lower pressure, and described bloating plant also is connected with fractionating column so that supply described expanded gas flow at tower middle part feed entrance point;(c) device for transferring is connected to discharge with the upper area of described fractionating column and distillates air-flow;(d) compression device is connected with described device for transferring to receive and describedly distillates air-flow and with its compression;(e) thus described heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough at least partial condensation and forming condensate flow of described compression, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(f) shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described shunting device also is connected with described fractionating column so that supply described reflux stream at the cat head feed entrance point to described fractionating column; With(g) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 34. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) first shunting device receives described liquefied natural gas and it is divided into first logistics and second logistics at least;(b) first bloating plant, be connected with described first shunting device and receive described first logistics and to make it to be expanded to lower pressure, described first bloating plant also connect the absorption tower in case at the bottom of first logistics that first tower middle part feed entrance point is supplied described expansion produces overhead gas stream and tower liquid stream;(c) heat-exchange apparatus, being connected to receive described second logistics and be heated to described first shunting device is enough to vaporize to small part;(d) second bloating plant, be connected second logistics that receives described heating with described heat-exchange apparatus and make it to be expanded to described lower pressure, described second bloating plant also is connected with described absorption tower so that second logistics after described expansion heating is supplied in the underfeed position;(e) the fractionation stripper is connected with described absorption tower so that liquid flows at the bottom of the cat head feed entrance point receives described tower;(f) first device for transferring is connected to discharge with the upper area of described fractionation stripper and distillates air-flow;(g) described heat-exchange apparatus also is connected with described first device for transferring to receive and describedly distillates air-flow and make it to be cooled to basic all condensations, and described cooling procedure is at least described second logistics a part of described heat effect is provided;(h) first pumping equipment, be connected with described heat-exchange apparatus and receive described basic condensate flow and to make it supercharging with pump, described first pumping equipment also is connected with described absorption tower so that at the described basic condensate flow with the pump supercharging of second tower middle part feed entrance point supply;(i) second device for transferring is connected with the upper area on described absorption tower and discharges overhead gas stream;(j) thus described heat-exchange apparatus also is connected with described second device for transferring to receive described overhead gas stream and make it to be cooled to and is enough to partial condensation at least and forms condensate flow, described cooling procedure is at least described second logistics a part of described heat effect is provided;(k) second pumping equipment is connected with described heat-exchange apparatus and receives described condensate flow and to make it supercharging with pump;(l) second shunting device, be connected the condensate flow that receives described pump supercharging with described second pumping equipment and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described second shunting device also is connected with described absorption tower so that supply described reflux stream at the cat head feed entrance point to described absorption tower; With(m) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 35. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus receives described liquefied natural gas and is heated;(b) first shunting device is connected the liquefied natural gas that receives after the described heating and it is divided into first logistics and second logistics at least with described heat-exchange apparatus;(c) first bloating plant, be connected with described first shunting device and receive described first logistics and to make it to be expanded to lower pressure, described first bloating plant be also connected on the absorption tower in case at the bottom of first logistics that first tower middle part feed entrance point is supplied described expansion produces overhead gas stream and tower liquid stream;(d) firing equipment, being connected to receive described second logistics and be heated to described first shunting device is enough to vaporize to small part;(e) second bloating plant, be connected second logistics that receives described heating with described firing equipment and make it to be expanded to described lower pressure, described second bloating plant also is connected with described absorption tower so that second logistics after described expansion heating is supplied in the underfeed position;(f) the fractionation stripper is connected with described absorption tower so that liquid flows at the bottom of the cat head feed entrance point receives described tower;(g) first device for transferring is connected to discharge with the upper area of described fractionation stripper and distillates air-flow;(h) described heat-exchange apparatus also is connected with described first device for transferring to receive and describedly distillates air-flow and make it to be cooled to basic all condensations, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(i) first pumping equipment, be connected with described heat-exchange apparatus and receive described basic condensate flow and to make it supercharging with pump, described first pumping equipment also is connected with described absorption tower so that supply the basic condensate flow of described pump supercharging at second tower middle part feed entrance point;(j) second device for transferring is connected with the upper area on described absorption tower and discharges overhead gas stream;(k) thus described heat-exchange apparatus also is connected with described second device for transferring to receive described overhead gas stream and make it to be cooled to and is enough at least partial condensation and forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(1) second pumping equipment is connected with described heat-exchange apparatus and receives described condensate flow and to make it supercharging with pump;(m) second shunting device, be connected with described second pumping equipment receive described with the pump supercharging condensate flow and it is divided into the described volatile liquid cut that comprises most of described methane and reflux stream at least, described second shunting device also is connected with described absorption tower so that supply described reflux stream at the cat head feed entrance point to described absorption tower; With(n) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 36. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus, receiving described liquefied natural gas and being heated to is enough to vaporize to small part;(b) bloating plant, be connected with described heat-exchange apparatus and receive the liquefied natural gas after the described heating and to make it to be expanded to lower pressure, described bloating plant be also connected on the absorption tower in case the liquefied natural gas after described expansion heating is supplied in the underfeed position produce overhead gas stream and tower at the bottom of liquid stream;(c) the fractionation stripper is connected with described absorption tower so that liquid flows at the bottom of the cat head feed entrance point receives described tower;(d) first device for transferring is connected to discharge with the upper area of described fractionation stripper and distillates air-flow;(e) compression device is connected with described first device for transferring to receive and describedly distillates air-flow and with its compression;(f) described heat-exchange apparatus also is connected with described compression device and receives distillating air-flow and make it to be cooled to and being enough to partial condensation at least of described compression, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided, and described heat-exchange apparatus also links to each other with described absorption tower so that supply the compression logistics of described cooling at tower middle part feed entrance point;(g) second device for transferring is connected with the upper area on described absorption tower and discharges described overhead gas stream;(h) thus described heat-exchange apparatus also is connected with described second device for transferring to receive described overhead gas stream and make it to be cooled to and is enough at least partial condensation and forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(i) pumping equipment is connected with described heat-exchange apparatus and receives described condensate flow and to make it supercharging with pump;(j) second shunting device, be connected with described pumping equipment to receive and describedly be divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least with the condensate flow of pump supercharging and with it, described second shunting device also is connected with described absorption tower so that supply described reflux stream at the cat head feed entrance point to described absorption tower; With(k) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 37. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus, receiving described liquefied natural gas and being heated to is enough to small part vaporization;(b) bloating plant, be connected with described heat-exchange apparatus and receive the liquefied natural gas after the described heating and to make it to be expanded to lower pressure, described bloating plant be also connected on the absorption tower in case the liquefied natural gas after described expansion heating is supplied in the underfeed position produce overhead gas stream and tower at the bottom of liquid stream;(c) the fractionation stripper is connected with described absorption tower so that liquid flows at the bottom of the cat head feed entrance point receives described tower;(d) first device for transferring is connected to discharge with the upper area of described fractionation stripper and distillates air-flow;(e) described heat-exchange apparatus also is connected with described first device for transferring to receive and describedly distillates air-flow and make it to be cooled to basic all condensations, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(f) first pumping equipment is connected with described heat-exchange apparatus and receives described basic condensate flow and to make it supercharging with pump, and described first pumping equipment also is connected with described absorption tower so that at the described basic condensate flow with the pump supercharging of tower middle part feed entrance point supply;(g) second device for transferring is connected with the upper area on described absorption tower and discharges overhead gas stream;(h) thus described heat-exchange apparatus also is connected with described second device for transferring to receive described overhead gas stream and make it to be cooled to and is enough at least partial condensation and forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(i) second pumping equipment is connected with described heat-exchange apparatus and receives described condensate flow and to make it supercharging with pump;(j) second shunting device, be connected with described second pumping equipment to receive and describedly be divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least with the condensate flow of pump supercharging and with it, described second shunting device also is connected with described absorption tower so that supply described reflux stream at the cat head feed entrance point to described absorption tower; With(k) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 38. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus, receiving described liquefied natural gas and being heated to is enough to the part vaporization;(b) separation equipment is connected the logistics that receives the vaporization of described heating rear section and makes it to be separated into air-flow and liquid stream with described heat-exchange apparatus;(c) first bloating plant, be connected with described separation equipment and receive described air-flow and to make it to be expanded to lower pressure, described first bloating plant be also connected on the absorption tower in case the first underfeed position supply described expanded gas flow produce overhead gas stream and tower at the bottom of liquid stream;(d) second bloating plant is connected with described separation equipment and receives described liquid stream and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described absorption tower so that supply described inflation fluid in the second underfeed position and flows;(e) the fractionation stripper is connected with described absorption tower so that liquid flows at the bottom of the cat head feed entrance point receives described tower;(f) first device for transferring is connected to discharge with the upper area of described fractionation stripper and distillates air-flow;(g) first compression device is connected with described first device for transferring to receive and describedly distillates air-flow and with its compression;(h) described heat-exchange apparatus also is connected with described first compression device and receives distillating air-flow and make it to be cooled to and being enough to partial condensation at least of described compression, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided, and described heat-exchange apparatus also links to each other with described absorption tower so that supply the compression logistics of described cooling at tower middle part feed entrance point;(i) second device for transferring is connected with the upper area on described absorption tower and discharges described overhead gas stream;(j) second compression device is connected with described second device for transferring and receives described overhead gas stream and with its compression;(k) thus described heat-exchange apparatus also is connected the overhead gas stream that receives described compression with described second compression device and makes it to be cooled to and is enough at least partial condensation and forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(l) second shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described second shunting device also is connected with described absorption tower so that supply described reflux stream at the cat head feed entrance point to described absorption tower; With(m) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 39. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus, receiving described liquefied natural gas and being heated to is enough to vaporize to small part;(b) bloating plant, be connected with described heat-exchange apparatus and receive the liquefied natural gas after the described heating and to make it to be expanded to lower pressure, described bloating plant also connect the absorption tower in case the liquefied natural gas after described expansion heating is supplied in the underfeed position produce overhead gas stream and tower at the bottom of liquid stream;(c) the fractionation stripper is connected with described absorption tower so that liquid flows at the bottom of the cat head feed entrance point receives described tower;(d) first device for transferring is connected to discharge with the upper area of described fractionation stripper and distillates air-flow;(e) first compression device is connected with described first device for transferring to receive and describedly distillates air-flow and with its compression;(f) described heat-exchange apparatus also is connected with described first compression device and receives distillating air-flow and make it to be cooled to and being enough to partial condensation at least of described compression, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided, and described heat-exchange apparatus also is connected with described absorption tower so that supply the compression logistics of described cooling at tower middle part feed entrance point;(g) second device for transferring is connected with the upper area on described absorption tower and discharges overhead gas stream;(h) second compression device is connected with described second device for transferring and receives described overhead gas stream and with its compression;(i) thus described heat-exchange apparatus also is connected with described second device for transferring to receive described overhead gas stream and make it to be cooled to and is enough at least partial condensation and forms condensate flow, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(j) shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described shunting device also is connected with described absorption tower so that supply described reflux stream at the cat head feed entrance point to described absorption tower; With(k) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 40. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus, receiving described liquefied natural gas and being heated to is enough to the part vaporization;(b) separation equipment is connected the logistics that receives the vaporization of described heating rear section and makes it to be separated into air-flow and liquid stream with described heat-exchange apparatus;(c) first bloating plant, be connected with described separation equipment and receive described air-flow and to make it to be expanded to lower pressure, described first bloating plant also connect the absorption tower in case the first underfeed position supply described expanded gas flow produce overhead gas stream and tower at the bottom of liquid stream;(d) second bloating plant is connected with described separation equipment and receives described liquid stream and to make it to be expanded to described lower pressure, and described second bloating plant also is connected with described absorption tower so that supply described inflation fluid in the second underfeed position and flows;(e) pumping equipment is connected with described absorption tower and receives at the bottom of the described tower liquid stream and to make it supercharging with pump;(f) fractionation stripper and described pumping equipment are connected in the cat head feed entrance point mutually and receive described with liquid stream at the bottom of the tower of pump supercharging;(g) first device for transferring is connected to discharge with the upper area of described fractionation stripper and distillates air-flow;(h) described heat-exchange apparatus also be connected with described first device for transferring receive described distillate air-flow and make it to be cooled to be enough to partial condensation at least, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided, and described heat-exchange apparatus also links to each other with described absorption tower so that supply the logistics that distillates of described cooling at tower middle part feed entrance point;(i) second device for transferring is connected with the upper area on described absorption tower and discharges described overhead gas stream;(j) compression device is connected with described second device for transferring and receives described overhead gas stream and with its compression;(k) thus described heat-exchange apparatus also is connected the overhead gas stream that receives described compression and makes it to be cooled to and is enough at least partial condensation and forms condensate flow with described compression device, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(l) shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described shunting device also is connected with described absorption tower so that supply described reflux stream at the cat head feed entrance point to described absorption tower; With(m) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 41. one kind be used for comprise methane and more the liquefied natural gas of heavy hydrocarbon component be separated into the volatile liquid cut that comprises most of described methane and comprise the device of the low volatility liquid distillate of most of described more heavy hydrocarbon component, comprise(a) heat-exchange apparatus, receiving described liquefied natural gas and being heated to is enough to vaporize to small part;(b) bloating plant, be connected the logistics that receives the vaporization of described heating rear section with described heat-exchange apparatus and make it to be expanded to lower pressure, described bloating plant also connect the absorption tower in case the liquefied natural gas of supplying described expansion heating in the underfeed position produce overhead gas stream and tower at the bottom of liquid stream;(c) pumping equipment is connected with described absorption tower and receives at the bottom of the described tower liquid stream and to make it supercharging with pump;(d) fractionation stripper and described pumping equipment are connected in the cat head feed entrance point mutually and receive described with liquid stream at the bottom of the tower of pump supercharging;(e) first device for transferring is connected to discharge with the upper area of described fractionation stripper and distillates air-flow;(f) described heat-exchange apparatus also be connected with described first device for transferring receive described distillate air-flow and make it to be cooled to be enough to partial condensation at least, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided, and described heat-exchange apparatus also is connected with described absorption tower so that supply the logistics that distillates of described cooling at tower middle part feed entrance point;(g) second device for transferring is connected with the upper area on described absorption tower and discharges described overhead gas stream;(h) compression device is connected with described second device for transferring and receives described overhead gas stream and with its compression;(i) thus described heat-exchange apparatus also is connected the overhead gas stream that receives described compression and makes it to be cooled to and is enough at least partial condensation and forms condensate flow with described compression device, described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided;(j) shunting device, be connected with described heat-exchange apparatus and receive described condensate flow and it is divided into described volatile liquid cut and the reflux stream that comprises most of described methane at least, described shunting device also is connected with described absorption tower so that supply described reflux stream at the cat head feed entrance point to described absorption tower; With(k) control appliance, the temperature that is suitable for the described feed stream regulating the amount and the temperature of described reflux stream and infeed described fractionating column is so that the tower top temperature of described fractionating column remains on uniform temperature, thereby reclaims most of described more heavy hydrocarbon component by fractionation in described low volatility liquid distillate.
- 42. the device of claim 26 or 28, wherein said heat-exchange apparatus also is connected with described second shunting device and receives described reflux stream and make it further cooling, described heat-exchange apparatus also is connected with described fractionating column so that supply the reflux stream of described further cooling at described cat head feed entrance point, and described cooling procedure is at least described second logistics a part of described heat effect is provided.
- 43. claim 27,29,30 or 31 device, wherein said heat-exchange apparatus also is connected with described second shunting device and receives described reflux stream and make it further cooling, described heat-exchange apparatus also is connected with described fractionating column so that supply the reflux stream of described further cooling at described cat head feed entrance point, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 44. the device of claim 32 or 33, wherein said heat-exchange apparatus also is connected with described shunting device and receives described reflux stream and make it further cooling, described heat-exchange apparatus also is connected with described fractionating column so that supply the reflux stream of described further cooling at described cat head feed entrance point, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 45. the device of claim 34, wherein said heat-exchange apparatus also is connected with described second shunting device and receives described reflux stream and make it further cooling, described heat-exchange apparatus also is connected with described absorption tower so that supply the reflux stream of described further cooling at described cat head feed entrance point, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 46. the device of claim 35, wherein said heat-exchange apparatus also is connected with described second shunting device and receives described reflux stream and make it further cooling, described heat-exchange apparatus also is connected with described absorption tower so that supply the reflux stream of described further cooling at described cat head feed entrance point, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 47. claim 36,37,38,39,40 or 41 device, wherein said heat-exchange apparatus also is connected with described shunting device and receives described reflux stream and make it further cooling, described heat-exchange apparatus also is connected with described absorption tower so that supply the reflux stream of described further cooling at described cat head feed entrance point, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 48. the device of claim 37, wherein said heat-exchange apparatus also be connected with described first pumping equipment receive described with the pump supercharging basic condensate flow and be heated, described heat-exchange apparatus also is connected with described absorption tower so that supply described heating and with the logistics of pump supercharging at described tower middle part feed entrance point, and described heating process is at least and describedly distillates air-flow or described overhead gas stream provides a part of described cooling effect.
- 49. the device of claim 48, wherein said heat-exchange apparatus also is connected with described second shunting device and receives described reflux stream and make it further cooling, described heat-exchange apparatus also is connected with described absorption tower so that supply the reflux stream of described further cooling at described cat head feed entrance point, and described cooling procedure is at least described liquefied natural gas a part of described heat effect is provided.
- 50. claim 26,27,28 or 29 device, wherein(1) second heat-exchange apparatus is connected with described second shunting device and receives described reflux stream and make it further cooling, and described second heat-exchange apparatus also is connected with described fractionating column so that supply the reflux stream of described further cooling at described cat head feed entrance point; With(2) described second heat-exchange apparatus also is connected first logistics that receives described expansion with described first bloating plant and is heated, described second heat-exchange apparatus also is connected with described fractionating column so that in described first logistics that adds thermal expansion of described first tower middle part feed entrance point supply, described heating process is at least described reflux stream provides a part described further cooling effect.
- 51. the device of claim 34 or 35, wherein(1) second heat-exchange apparatus is connected with described second shunting device and receives described reflux stream and make it further cooling, and described second heat-exchange apparatus also is connected with described absorption tower so that supply the reflux stream of described further cooling at described cat head feed entrance point; With(2) described second heat-exchange apparatus also is connected first logistics that receives described expansion with described first bloating plant and is heated, described second heat-exchange apparatus also is connected with described absorption tower so that in described first logistics that adds thermal expansion of described first tower middle part feed entrance point supply, described heating process is at least described reflux stream provides a part described further cooling effect.
- 52. the device of claim 34 or 35, wherein(1) second heat-exchange apparatus is connected with described second shunting device and receives described reflux stream and make it further cooling, and described second heat-exchange apparatus also is connected with described absorption tower so that supply the reflux stream of described further cooling at described cat head feed entrance point; With(2) described second heat-exchange apparatus also be connected with described first pumping equipment receive described with the pump supercharging basic condensate flow and be heated, described second heat-exchange apparatus also is connected with described absorption tower so that supply described heating and with the basic condensate flow of pump supercharging, described heating process is at least described reflux stream a part of described further cooling effect is provided at described second tower middle part feed entrance point.
- 53. claim 1,2,3,4,5,6,7,8,9,10,11,12,13,14,15,16,19,21 or 22 method wherein reclaim most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 54. the method for claim 17 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 55. the method for claim 18 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 56. the method for claim 20 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 57. the method for claim 23 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 58. the method for claim 24 wherein reclaims described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 59. the method for claim 25 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 60. claim 26,27,28,29,30,31,32,33,34,35,36,37,38,39,40,41,45,46,48 or 49 device wherein reclaim described methane and C in described volatile liquid cut 2The major part of component reclaims C in described low volatility liquid distillate 3Component reaches the more major part of heavy hydrocarbon component.
- 61. the device of claim 42 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 62. the device of claim 43 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 63. the device of claim 44 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 64. the device of claim 47 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 65. the device of claim 50 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 66. the device of claim 51 wherein reclaims most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
- 67. the device of claim 52 is wherein reclaiming most of described methane and C in described volatile liquid cut 2Component reclaims most of C in described low volatility liquid distillate 3Component reaches more heavy hydrocarbon component.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US58466804P | 2004-07-01 | 2004-07-01 | |
| US60/584,668 | 2004-07-01 | ||
| US60/646,903 | 2005-01-24 | ||
| US60/669,642 | 2005-04-08 | ||
| US60/671,930 | 2005-04-15 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1954186A CN1954186A (en) | 2007-04-25 |
| CN100436988C true CN100436988C (en) | 2008-11-26 |
Family
ID=38059740
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005800147024A Active CN100436988C (en) | 2004-07-01 | 2005-06-03 | Liquefied natural gas processing |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100436988C (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090282865A1 (en) * | 2008-05-16 | 2009-11-19 | Ortloff Engineers, Ltd. | Liquefied Natural Gas and Hydrocarbon Gas Processing |
| US8584488B2 (en) * | 2008-08-06 | 2013-11-19 | Ortloff Engineers, Ltd. | Liquefied natural gas production |
| US8434325B2 (en) * | 2009-05-15 | 2013-05-07 | Ortloff Engineers, Ltd. | Liquefied natural gas and hydrocarbon gas processing |
| US20100287982A1 (en) * | 2009-05-15 | 2010-11-18 | Ortloff Engineers, Ltd. | Liquefied Natural Gas and Hydrocarbon Gas Processing |
| CN104628505B (en) * | 2013-11-15 | 2016-09-07 | 中国石油天然气股份有限公司 | A kind of method and device reclaiming ethane from liquefied natural gas |
| JP6527714B2 (en) * | 2015-02-25 | 2019-06-05 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Liquid fuel gas supply apparatus and supply method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1535846A (en) * | 1966-08-05 | 1968-08-09 | Shell Int Research | Process for the separation of mixtures of liquefied methane |
| US5114451A (en) * | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
| CN1212756A (en) * | 1996-02-29 | 1999-03-31 | 国际壳牌研究有限公司 | Method of reducing amount of components having low boiling points in liquefied natural gas |
| US20030158458A1 (en) * | 2002-02-20 | 2003-08-21 | Eric Prim | System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas |
| US20030188996A1 (en) * | 2002-04-03 | 2003-10-09 | Kenneth Reddick | Liquid natural gas processing |
-
2005
- 2005-06-03 CN CNB2005800147024A patent/CN100436988C/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1535846A (en) * | 1966-08-05 | 1968-08-09 | Shell Int Research | Process for the separation of mixtures of liquefied methane |
| US5114451A (en) * | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
| CN1212756A (en) * | 1996-02-29 | 1999-03-31 | 国际壳牌研究有限公司 | Method of reducing amount of components having low boiling points in liquefied natural gas |
| US20030158458A1 (en) * | 2002-02-20 | 2003-08-21 | Eric Prim | System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas |
| US20030188996A1 (en) * | 2002-04-03 | 2003-10-09 | Kenneth Reddick | Liquid natural gas processing |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1954186A (en) | 2007-04-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100406832C (en) | Liquefied natural gas processing | |
| CN100516734C (en) | Cryogenic liquid natural gas recovery process | |
| CN102027304B (en) | Liquefied natural gas and hydrocarbon gas processing | |
| JP4447639B2 (en) | Treatment of liquefied natural gas | |
| CN102428334B (en) | Liquefied natural gas and hydrocarbon gas processing | |
| CN101460800B (en) | Liquefied natural gas processing | |
| CN102428333B (en) | Liquefied natural gas and hydrocarbon gas processing | |
| AU607870B2 (en) | Ethane recovery system | |
| CN101233376B (en) | Liquid natural gas processing method | |
| KR101687852B1 (en) | Hydrocarbon gas processing | |
| CN101652619B (en) | Liquefied natural gas processing | |
| MX2007015226A (en) | Hydrocarbon gas processing. | |
| CN100473927C (en) | Natural gas liquefaction method and device | |
| EA005326B1 (en) | Natural gas liquefaction | |
| WO2002014242A1 (en) | Hydrocarbon gas processing | |
| WO1996040604A1 (en) | Hydrocarbon gas processing | |
| EA011919B1 (en) | Natural gas liquefaction | |
| KR20120069729A (en) | Hydrocarbon gas processing | |
| CN100436988C (en) | Liquefied natural gas processing | |
| AU710661C (en) | Hydrocarbon gas processing | |
| MXPA06014200A (en) | Liquefied natural gas processing |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200109 Address after: Illinois, USA Patentee after: UOP LLC Address before: Texas, USA Patentee before: Ortloff Engeneers Ltd. |
|
| TR01 | Transfer of patent right |