JP2013524149A5 - - Google Patents

Description

Distillation vapor stream is withdrawn from the upper region of the deethanizer zone is cooled by heat exchange with the top vapor stream from the absorption zone. As a result, at least a portion of the distillation vapor stream is condensed. The condensed liquid is separated from the cooled distilled vapor stream, resulting in a cryogenic liquid reflux stream that is directed to the upper region of the absorption zone. In this upper region, the cryogenic liquid can contact the vapor portion of the expanded stream, as described above. Vapor portion of the cooled distillation vapor stream (if present case is) top vapor from and absorption zone is mixed, residual methane and C ₂ components product gas is formed.

Deethanizer in fractionation tower 15, the tray away plurality of vertically, which is a conventional distillation column with one or more packed beds or trays and some combination of the packing. The deethanizer tower consists of two zones, an upper absorption (rectification) zone 15a and a lower removal zone 15b. Incidentally, upper absorbing (rectification) section 15a, in order to condense and absorb the C ₃ components and heavier components, necessary contact between the vapor portion of the expanded stream 34a rises, the low-temperature liquid to fall The lower removal zone 15b comprises a tray and / or packing that provides the necessary contact between the falling liquid and the rising vapor. The deethanizing section 15b comprises at least one reboiler (such as the reboiler 16). This reboiler provides removed steam by heating and evaporating a portion of the liquid flowing down the column. This removal vapor removes the liquid product or stream 37 from the methane, C ₂ component, and lighter components by flowing up the column. Stream 34 a flows into deethanizer 15 at a central column feed point located in the region below absorption zone 15 a of deethanizer 15. The liquid portion of the expanded stream 34a mixes with the liquid falling from the absorption zone 15a, and this mixture continues to fall into the removal zone 15b of the deethanizer 15. The vapor portion of the expanded stream 34a rises through the absorption zone 15a and contacts the falling cryogen. As a result, C ₃ components and heavier components are condensed and absorbed.

Some of the distillation vapor (stream 38) is withdrawn from the upper region of the removal area 15b. This stream is then cooled and partially condensed in exchanger 17 by heat exchange with the cryogenic deethanizer top stream 36 exiting from the top of deethanizer 15 at -109 degrees Fahrenheit (-79 degrees Celsius). (Stream 38a). The cryogenic deethanizer top stream cools stream 38 from -30 degrees Fahrenheit (-35 degrees Celsius) to about -103 degrees Fahrenheit (-75 degrees Celsius) (stream 38a) and about -33 degrees Fahrenheit (Celsius- 66 degrees) (stream 36a).

The operating pressure in the reflux separator 18 is maintained at a pressure slightly lower than the operating pressure of the deethanizer 15. This pressure difference, distillation vapor stream 38 passes through heat exchanger 17, so that the driving force that allows the flow to the reflux separator 18 is produced. In the reflux separator 18, the condensed liquid (stream 40) is separated from the non-condensed vapor (stream 39). Non-condensed vapor stream 39 mixes with warmed deethanizer top stream 36a emanating from exchanger 17, resulting in the formation of a cold residual gas stream 44 of -37 degrees Fahrenheit (-38 degrees Celsius). .

The liquid stream 40 emanating from the reflux separator 18 is ejected by the pump 19 and becomes a pressure slightly higher than the operating pressure of the deethanizer 15. The resulting stream 40a is then split into two parts. The first part (stream 41) is provided as a cold upper column feed (circulation) in the upper region of the absorption zone 15a of the deethanizer 15. Due to this low-temperature liquid, an absorption cooling effect occurs in the absorption (rectification) zone 15 a of the deethanizer 15. In this absorption cooling effect, the area 15a is cooled by saturation of the vapor rising in the tower due to evaporation of liquid methane and ethane contained in the stream 41. As a result, both the vapor that escapes the upper region of the absorption zone 15a (the top stream 36) and the liquid that escapes the lower zone (the distillate stream 43) are fed into any of the feed streams (stream 41 and stream) flowing into the absorption zone 15a Note that the temperature is lower than 34a). This absorption cooling effect allows the top of the column (stream 36) to partially condense the distilled vapor stream (stream 38) without operating the removal zone 15b at a pressure significantly higher than the pressure in the absorption zone 15a. It becomes possible to provide the cooling required in the heat exchanger 17. This absorption cooling effect, reflux stream 41, is also promoted to condense and absorb the C ₃ components and heavier components in the distillation vapor rising through the absorbing region 15a. The second part (stream 42) of the jetted stream 40a is supplied to the upper region of the removal zone 15b of the deethanizer 15. It should be noted that in the removal zone 15b, the cryogenic liquid acts as a reflux for absorbing and condensing C ₃ and heavier components flowing from below to above, so that the distilled vapor stream 38 removes these components. The minimum amount will be included.

Separator section 115e has an internal head or other means of dividing separator section 115e from deethanization section 115d so that these two sections in processing assembly 115 can operate at different pressures. is there. The first portion of stream 31 (stream 32) flows into the lower region of separator section 115e at 875 psia (6,031 kPa (a)). In the separator section 115e, the condensed liquid is separated from the vapor before the vapor is guided to the heat / mass transfer means in the separator section 115e. This heat and mass transfer means is also a finned tube heat exchanger, plate heat exchanger, aluminum brazed heat exchanger, or other types of heat exchange devices including multi-path and / or multi-functional heat exchangers It may consist of. The heat / mass transfer means comprises a vapor portion of stream 32 flowing upward through one path of the heat / mass transfer means and a distillate stream 43 flowing downward from an absorption zone 115c within the processing assembly 115. It is configured to cool the steam while heating the distillate stream by performing heat exchange between them. As the steam stream is cooled, a portion of the steam stream is condensed and dropped while the remaining steam continues to flow upward through the heat and mass transfer means. The heat / mass transfer means also performs the function of transferring the mass between the vapor phase and the liquid phase by continuously bringing the condensed liquid and the vapor into contact with each other. As a result, a part of the steam is rectified.

A second portion of stream 31 (stream 33) flows into separator section 115e in processing assembly 115 above the heat and mass transfer means. All condensed liquid is separated from the vapor and mixed with all of the condensed liquid from the vapor portion of stream 32 flowing upward through the heat and mass transfer means. The vapor portion of stream 33 mixes with the vapor that escapes the heat and mass transfer means, resulting in the formation of stream 34. This stream 34 exits separator zone 115e at -31 degrees Fahrenheit (-35 degrees Celsius). Stream 35 is formed when the liquid portion of stream 32 and stream 33 (if present) and any liquid condensed from the vapor portion of stream 32 in the heat and mass transfer means are mixed. This stream 35 exits the separator zone 115e at -15 degrees Fahrenheit (-26 degrees Celsius). Stream 35 is expanded by expansion valve 12 to a pressure slightly above the operating pressure of deethan zone 115d in processing assembly 115 (approximately 383 psia (2,639 kPa (a))), and stream 35a is -42 degrees Fahrenheit. It is cooled to (41 degrees Celsius). As stream 35a flows into the heat exchange means in feed cooling zone 115a, it cools the feed gas as described above and stream 35b is fed to deethan zone 115d in processing assembly 115 at the lower center column feed point. Before, the stream 35b is heated to 103 degrees Fahrenheit (39 degrees Celsius).

Absorption zone 115c comprises absorbing means consisting of a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing. The trays and / or packings in the absorption area 115c provide the necessary contact between the rising vapor and the falling cryogenic liquid. The vapor portion of the expanded stream 34a rises through the absorbing means in the absorption zone 115c and contacts the falling cryogenic liquid. As a result, C ₃ components and heavier majority of components from these vapors are condensed and absorbed. The liquid portion of the expanded stream 34a mixes with liquid falling from the absorbing means in the absorption zone 115c, resulting in the formation of a distillate stream 43. Distillate stream 43 is drawn from the lower region of absorption zone 115c at -102 degrees Fahrenheit (-74 degrees Celsius). The distillate is heated to -9 degrees Fahrenheit (-23 degrees Celsius) while cooling the vapor portion of stream 32 in separator section 115e as described above. The heated distillate stream 43a is then fed to a deethanization zone 115d in the processing assembly 115 at the upper center column feed point. Generally, this liquid flow emanating from the absorption zone 115c, passing through the heat and mass transfer means in the separator zone 115e and reaching the deethanization zone 115d is due to thermosyphon circulation, but a pump may be used.

Absorption zone 115c has an internal head or other means of dividing absorption zone 115c from deethanization zone 115d so that these two zones in processing assembly 115 are slightly less than the pressure in absorption zone 115c. Operation is possible at high deethanizing zone 115d pressure. This pressure differential, drive first distillation vapor stream (stream 38) that is drawn from the upper area of the deethanizer section 115 d, allowing it to be guided to the heat exchange means of the condensation zone 115b of the processing assembly 115 Power will be generated. This heat exchange means is likewise a finned tube heat exchanger, a plate heat exchanger, an aluminum brazed heat exchanger, or other types of heat exchange including multi-path and / or multi-function heat exchangers It may consist of a device. Heat exchange means to perform a first distillation vapor stream 38 flowing through one path of the heat exchange means, heat exchange between the second distillation vapor stream rising from the absorption zone 115c of the processing assembly 115 It is configured. Then, the second distillation vapor stream, while to and at least partially condensed by cooling the stream 38, is heated. Then, the second distillation vapor stream flows from the heat exchange means, is separated into vapor and liquid phases. When the vapor phase (if present) is mixed with the heated second distillation vapor stream exiting the heat exchange means, a residual gas stream is formed. This residual gas stream is cooled in the feed cooling zone 115a as described above. The liquid phase is divided into two parts: stream 41 and stream 42.

The first portion (stream 41) is fed as a cold upper column feed (circulation) by gravity flow into the region above the absorption zone 115c in the processing assembly 115. Due to this low temperature liquid, an absorption cooling effect occurs in the absorption (rectification) zone 115a. In this absorption cooling effect, the absorption zone 115c is cooled by saturation of the vapor rising in the tower due to evaporation of liquid methane and ethane contained in the stream 41. This absorption cooling effect, the second distillation vapor stream is significantly higher without operating the deethanizer zone 115d in pressure than the absorption zone 115c, the first distillation vapor stream (stream 38) partially condensed In doing so, it is possible to provide the cooling required in the heat exchange means of the condensation zone 115b. This absorption cooling effect, reflux stream 41, is also promoted to condense and absorb the C ₃ components and heavier components in the distillation vapor rising through the absorbing section 115c. The second portion (stream 42) of the liquid phase separated in the condensation zone 115b is fed as a cold upper column feed (circulation) by gravity flow into the region above the deethanization zone 115d in the processing assembly 115. it allows cryogenic liquid, serves as reflux for absorbing and condensing the C ₃ components and heavier components rising from below. As a result, distillation vapor stream 38 will contain these ingredients in the minimum amount.

The deethanization zone 115d in the processing assembly 115 comprises mass transfer means consisting of a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing. The tray and / or packing in the deethanizing zone 115d provides the necessary contact between the rising vapor and the falling liquid. Deethanizer zone 115d also comprises a heat-mass transfer means below the mass transfer means. This heat and mass transfer means is also a finned tube heat exchanger, plate heat exchanger, aluminum brazed heat exchanger, or other types of heat exchange devices including multi-path and / or multi-functional heat exchangers It may consist of. The heat / mass transfer means exchanges heat between the heating medium flowing through one path of the heat / mass transfer means and the distillate stream flowing downward from the mass transfer means in the deethanizing section 115d. Thus, the distillate stream is configured to be heated. As the distillate stream is heated, a portion of the distillate stream evaporates and a rising removal vapor is formed. This removed vapor rises as the remaining liquid continues to fall through the heat and mass transfer means. Heat and mass transfer means, the removal vapor and distillation liquid stream is continuously contacted, thereby also performs function of performing mass transfer between the vapor and liquid phases. As a result, the liquid product stream 37 is removed from the methane, C ₂ component, and lighter components. The resulting liquid product (stream 37) exits the lower region of deethanization zone 115d and exits processing assembly 115 at 203 degrees Fahrenheit (95 degrees Celsius).

The second distillation vapor stream rising from the absorption zone 115c is warmed in the condensation zone 115b as the stream 38 is cooled as described above. The second distillation vapor stream warmed, as described above, it is mixed with all of the steam separated from the first distillation vapor stream 38 which is cooled. The resulting residual gas stream is heated in the feed cooling zone 115a as the stream 31 is cooled as described above. The residual gas stream 44 then exits the processing assembly 115 at 104 degrees Fahrenheit (40 degrees Celsius). The residual gas stream is then recompressed by two stages: a compressor 14 driven by an expander 13 and a compressor 20 driven by an auxiliary power source. After cooling to 120 degrees Fahrenheit (49 degrees Celsius) in the discharge cooler 21, the residual gas stream 44c is 915 psia (6,307 kPa (a)) that fully meets the line requirements (usually the degree of inlet pressure) It flows to the sales gas pipeline.

Second, using the heat / mass transfer means in the deethanization zone 115d, the distillate flowing out of the mass transfer means in the deethanization zone 115d is heated, and at the same time, the resulting vapor comes into contact with the distillate and its volatile components. Is more efficient than using a conventional distillation column with an external reboiler. Volatile components are continuously removed from the distillate, and the concentration of volatile components in the removed steam is more quickly reduced. As a result, the removal efficiency related to the present invention is improved.

Thirdly, the stream 34 is first partially rendered by using heat and mass transfer means in the separator section 115e to cool the vapor portion of the stream 32 while condensing heavier hydrocarbon components from the vapor. It is rectified and then expanded and fed as a feed to the absorption zone 115c. As a result, as seen by comparing the flow rates of stream 41 in Tables 1 and 2, in removing C ₃ and heavier hydrocarbon components from stream 34a by rectifying expanded stream 34a. Less reflux (stream 41) will be required.

As described above with respect to the embodiment of the present invention shown in FIG. 2, the first distillation vapor stream 38 is partially condensed, the resulting condensed water from the steam flowing out from the operating expander, valuable C Used to absorb _three and heavier components. However, the present invention is not limited to this embodiment. In cases where other design considerations indicate that the expander output or a portion of the condensate should bypass the absorption area 115c of the processing assembly 115, for example, the discharge emanating from the operational expander in this way It may be advantageous to treat only a part of the steam, or it may be advantageous to use only a part of the condensed water as the absorbent. Feed gas conditions, plant scale, available equipment, or other factors may indicate that the operational expander 13 can be eliminated or replaced with an alternative expansion device (such as an expansion valve) , Allowing (or not partially) condensing of the first distillation vapor stream 38 in the condensation section 115b (FIGS. 2-13) or heat exchanger 17 (FIGS. 14-21) in the processing assembly 115 May also be shown. By the composition of the feed gas stream, in the condensation zone 115b (FIGS. 13), or in the heat exchanger 17 (FIGS. 14 to 21), in order to the first distillation vapor stream 38 is partially cooled, It should be noted that it may be advantageous to use external cooling.

In some situations, it may be advantageous to use an external separation tank to separate the cooled first portion 32 and second portion 33 or the cooled feedstream 31a, rather than including a separator section 115e in the processing assembly 115. There can be. As shown in FIGS. 8 and 18, heat / mass transfer means in the separator 11 may be used to separate the cooled first portion 32 and second portion 33 into a vapor stream 34 and a liquid stream 35. Good. Similarly, separator 11 can be used to separate cooled feed stream 31a into vapor stream 34 and liquid stream 35, as shown in FIGS. 9-13 and 19-21.

The liquid stream 35 emanating from the separator section 115e or the separator 11 and the distillate stream 43 emanating from the absorption section 115c are used and distributed for process heat exchange, feed gas (streams 31 and / or 32) and second The particular configuration of the heat exchanger for cooling one distillation steam stream 38 and the selection of the treatment stream for a particular heat exchange function must be evaluated for each particular application. For example, in FIGS. 4-6, 10-12, 16 and 20, in the condensation zone 115b (FIGS. 4, 5, 10 and 11), the heat exchanger 10 (FIGS. 6 and in 12) or heat exchanger 17 (FIG. 16 and FIG. 20), it is shown that using the distillate stream 43 of the first distillation vapor stream 38 to partially cooled. In such cases, heat and mass transfer means may not be required in the separator section 115e (FIGS. 4-6 and 16) or in the separator 11 (FIGS. 10-12 and 20). In the embodiment shown in FIGS. 4 and 10, the pump 22 is used to deliver the distillate stream 43 to the heat exchange means in the condensation zone 115b. In the embodiment shown in FIGS. 5 and 11, the condensation zone 115b is located below the absorption zone 115c in the processing assembly 115 so that the flow of the distillate stream 43 is due to thermosiphon circulation. In the embodiment shown in FIGS. 6 and 12, a heat exchanger 10 located outside the processing assembly 115 is used, and the feed cooling zone 115a is located below the absorption zone 115c in the processing assembly 115, so that The flow of the distillate stream 43 is due to thermosiphon circulation. (In the embodiment shown in FIGS. 5, 6, 11, and 12, the reflux is provided at a point in the processing assembly 115 above the point where the liquid phase condensed from the stream 38 is collected. A reflux pump 19 is used to supply.) In the embodiment shown in FIGS. 16 and 20, the distillate stream 43 can flow sufficiently through the heat exchanger 17 by the action of thermosyphon circulation. It is possible or may be necessary for the pump 22 to circulate the stream 43. In some situations, distillate stream 43 may be used to cool stream 32 in a heat exchanger located external to processing assembly 115, such as heat exchanger 10 shown in FIGS. 3, 9, 15, and 19. It may be preferable to use In still other situations, the distillate stream 43 is not heated at all, and instead, as shown in FIGS. 7, 13, 17, and 21, the distillate stream 43 is moved to the upper region of the deethanization zone 115d. In some cases, it may be preferred to use as a reflux. (For the embodiment shown in FIGS. 13 and 21, the pump 22 may be required because the stream 43 cannot flow due to gravity.)

According to the present invention, especially in the case of richness is high inlet gas, available input gas, and / or available cooling to the first distillation vapor stream emitted from the second distillation vapor stream and distillate streams External cooling may be used to supplement In such cases where additional inflow gas cooling is desired, the heat and mass transfer means may be located in the separator section 115e (or the cooled first as shown by the dotted lines in FIGS. 3-7 and 15-17). Gas collecting means in such a case where the part 32 and the second part 33 or the cooled feed stream 31a does not contain any liquid), and the heat / mass transfer means are shown in FIGS. It may be included in the separator 11 as shown by the dotted lines in FIGS. This heat and mass transfer means is also a finned tube heat exchanger, plate heat exchanger, aluminum brazed heat exchanger, or other types of heat exchange devices including multi-path and / or multi-functional heat exchangers It may consist of. The heat / mass transfer means performs heat exchange between the refrigerant stream (that is, propane) passing through one path of the heat / mass transfer means and the steam portion of the stream 31a flowing upward, so that the refrigerant Further cooling, condensing additional liquid, which is configured to fall and become part of the liquid removed in stream 35. Heat, mass transfer means in the separator section 115e (FIGS. 2 and 14) or in the separator 11 (FIGS. 8 and 18), as shown by the dotted lines in FIG. 2, FIG. 8, FIG. 14 and FIG. May include servicing to provide supplemental cooling using a refrigerant. Alternatively, conventional gas cooler (s) may be used before stream 32 and stream 33 flow into separator section 115e (FIGS. 2 and 14) or separator 11 (FIGS. 8 and 18), or Before stream 31a enters separator section 115e (FIGS. 3-7 and 15-17) or separator 11 (FIGS. 9-13 and 19-21), stream 32, stream 33, and / Or may be used to cool the stream 31a with a refrigerant. In case additional cooling of the first distillation vapor stream is desired, the condensation zone 115b of the processing assembly 115 (FIGS. 2 to 5 and 7 to 11 and 13), the heat exchanger 10 (FIGS. 6 and The heat exchange means in FIG. 12) or in the heat exchanger 17 (FIGS. 14-21) may comprise provisions for providing supplemental cooling with the refrigerant, as indicated by the dotted lines.

Depending on the type of heat exchanger selected for the heat exchange means in the feed cooling zone 115a and the condensation zone 115b (FIGS. 2-5, 7-11, and 13), these heat exchange means may be It may be possible to aggregate into a single multi-path and / or multi-functional heat exchange device. In such a case, the heat exchanger and / or multi-functional multi-path, in order to achieve the desired cooling and heating, stream 31, stream 32, stream 33, the first distillation vapor stream 38, cooled all of the steam separated from the stream 38, and the second distributing the distillation vapor stream will comprise separation, and suitable means for collecting.

Claims (31)

A gas stream containing methane, C ₂ component, C ₃ component, and heavier hydrocarbon component is separated into a volatile residual gas fraction and a relatively large volume containing the majority of the C ₃ component and heavier hydrocarbon component. A method for splitting into fractions of low volatility,
(1) cooling the gas stream in a first heat exchange means;
(2) expanding the cooled gas stream to a lower pressure, thereby further cooling;
(3) supplying the expanded, cooled gas stream as a bottom feed to an absorption means contained in a processing assembly;
(4) collecting the first distillate stream from the lower region of the absorption means and supplying it as an upper feed to the mass transfer means contained in the processing assembly;
(5) collecting the first distillation steam stream from the upper region of the mass transfer means, sufficiently cooling in the second heat exchange means, condensing at least a part of the first distillation steam stream;
(6) The at least partially condensed first distillation vapor stream is fed to a separation means and separated in the separation means, whereby the condensed stream and the first distillation vapor stream are cooled. Forming a residual vapor stream containing all the non-condensed vapor remaining behind,
(7) supplying at least a portion of the condensed stream as an upper feed to the absorption means;
(8) collecting at least part of the cooling of step (5) by collecting a second distillation vapor stream from the upper region of the absorption means and heating in the second heat exchange means;
(9) a second distillation vapor stream the heated and mixed with all of the residual vapor stream to form a mixed vapor stream,
(10) heating the mixed vapor stream in the first heat exchange means, thereby supplying at least a portion of the cooling of the step (1), and then supplying the heated mixed vapor stream to the volatile residue; Released as a gas fraction,
(11) a second distillate stream is heated in the heat-mass transfer means accommodated in said processing assembly collected from the lower region of the mass transfer means, whereby said components more volatile than the first Simultaneously removing from the distillate stream, then discharging the heated and removed second distillate stream from the processing assembly as the relatively less volatile fraction;
(12) The amount and temperature of the feed stream to the absorption means maintain the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively volatile fraction are recovered. Effective to do,
Method.   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ A process for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components comprising:
  (1) The gas stream is sufficiently cooled in the first heat exchange means, and the gas stream is partially condensed;
  (2) the partially condensed gas stream is fed to a first separation means and separated in the first separation means, so that a vapor stream and at least one liquid stream are provided;
  (3) the steam stream is expanded to a lower pressure, thereby further cooling;
  (4) the expanded, cooled vapor stream is fed as a bottom feed to an absorption means contained in a processing assembly;
  (5) the at least one liquid stream is expanded to the lower pressure;
  (6) The first distillate stream is collected from the lower region of the absorption means and supplied as an upper feed to the mass transfer means contained in the processing assembly;
  (7) The first distillation steam stream is collected from the upper region of the mass transfer means, and is sufficiently cooled in the second heat exchange means to condense at least a part of the first distillation steam stream,
  (8) The at least partially condensed first distillation vapor stream is fed to a second separation means and separated in the second separation means, whereby the condensed stream and the first distillation vapor stream A residual vapor stream containing all of the uncondensed vapor remaining after the is cooled,
  (9) At least a portion of the condensed stream is fed as an upper feed to the absorption means;
  (10) A second distillation vapor stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least a portion of the cooling of step (7);
  (11) The heated second distillation vapor stream is mixed with all of the residual vapor stream, resulting in the formation of a mixed vapor stream;
  (12) The mixed steam stream is heated in the first heat exchange means, thereby providing at least a portion of the cooling of step (1), and then the heated mixed steam stream is the volatile residue. Released as a gas fraction,
  (13) The expanded at least one liquid stream is heated in the first heat exchange means, thereby supplying at least a portion of the cooling of step (1) and then the heated expanded At least one liquid stream is fed to the mass transfer means as a bottom feed;
  (14) The second distillate stream is collected from the lower region of the mass transfer means and heated in the heat / mass transfer means accommodated in the processing assembly, whereby the more volatile components are removed from the first transfer stream. Simultaneously removing from the distillate stream, then discharging the heated and removed second distillate stream from the processing assembly as the relatively less volatile fraction;
  (15) The amount and temperature of the feed stream to the absorption means maintains the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively volatile fraction are recovered. Effective to do,
Method.   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ A process for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components comprising:
  (1) The gas stream is cooled in the first heat exchange means,
  (2) the cooled gas stream is expanded to a lower pressure, thereby further cooling;
  (3) the expanded, cooled gas stream is fed as a bottom feed to an absorption means contained in a processing assembly;
  (4) The first distillate stream is collected from the lower region of the absorption means and heated in the second heat exchange means, and the heated first distillate stream is then the substance contained in the processing assembly. Supplied to the vehicle as an upper or intermediate feed,
  (5) The first distillation vapor stream is collected from the upper region of the mass transfer means and is sufficiently cooled in the second heat exchange means to condense at least a portion of the first distillation vapor stream, thereby At least part of the heating of step (4) is provided;
  (6) The at least partially condensed first distillation vapor stream is fed to a separation means and separated in the separation means, whereby the condensed stream and the first distillation vapor stream are cooled. A residual vapor stream containing all of the uncondensed vapor remaining behind is formed,
  (7) At least a portion of the condensed stream is fed as an upper feed to the absorption means;
  (8) A second distillation vapor stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least a portion of the cooling of step (5);
  (9) the heated second distillation vapor stream is mixed with all of the residual vapor stream, resulting in a mixed vapor stream;
  (10) The mixed steam stream is heated in the first heat exchange means, thereby supplying at least a portion of the cooling of step (1), and then the heated mixed steam stream is the volatile residue. Released as a gas fraction,
  (11) The second distillate stream is collected from the lower region of the mass transfer means and heated in the heat / mass transfer means housed in the processing assembly, whereby the more volatile components are removed from the first transfer stream. Simultaneously removing from the distillate stream, then discharging the heated and removed second distillate stream from the processing assembly as the relatively less volatile fraction;
  (12) The amount and temperature of the feed stream to the absorption means maintain the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively volatile fraction are recovered. Effective to do,
Method.   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ A process for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components comprising:
  (1) The gas stream is sufficiently cooled in the first heat exchange means, and the gas stream is partially condensed;
  (2) the partially condensed gas stream is fed to a first separation means and separated in the first separation means, so that a vapor stream and at least one liquid stream are provided;
  (3) the steam stream is expanded to a lower pressure, thereby further cooling;
  (4) the expanded, cooled vapor stream is fed as a bottom feed to an absorption means contained in a processing assembly;
  (5) the at least one liquid stream is expanded to the lower pressure;
  (6) The first distillate stream is collected from the lower region of the absorption means and heated in the second heat exchange means, and the heated first distillate stream is then the substance contained in the processing assembly. Supplied to the vehicle as an upper or intermediate feed,
  (7) The first distillation vapor stream is collected from the upper region of the mass transfer means and sufficiently cooled in the second heat exchange means to condense at least a part of the first distillation vapor stream; Supplies at least part of the heating of step (6),
  (8) The at least partially condensed first distillation vapor stream is fed to a second separation means and separated in the second separation means, whereby the condensed stream and the first distillation vapor stream A residual vapor stream containing all of the uncondensed vapor remaining after the is cooled,
  (9) At least a portion of the condensed stream is fed as an upper feed to the absorption means;
  (10) A second distillation vapor stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least a portion of the cooling of step (7);
  (11) The heated second distillation vapor stream is mixed with all of the residual vapor stream, resulting in the formation of a mixed vapor stream;
  (12) The mixed steam stream is heated in the first heat exchange means, thereby providing at least a portion of the cooling of step (1), and then the heated mixed steam stream is the volatile residue. Released as a gas fraction,
  (13) The expanded at least one liquid stream is heated in the first heat exchange means, thereby supplying at least a portion of the cooling of step (1) and then the heated expanded At least one liquid stream is fed to the mass transfer means as a bottom feed;
  (14) The second distillate stream is collected from the lower region of the mass transfer means and heated in the heat / mass transfer means accommodated in the processing assembly, whereby the more volatile components are removed from the first transfer stream. Simultaneously removing from the distillate stream, then discharging the heated and removed second distillate stream from the processing assembly as the relatively less volatile fraction;
  (15) The amount and temperature of the feed stream to the absorption means maintains the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively volatile fraction are recovered. Effective to do,
Method.   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ A process for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components comprising:
  (1) The gas stream is partially cooled in the first heat exchange means,
  (2) the partially cooled gas stream is divided into a first part and a second part;
  (3) The first part is further cooled in the first heat / mass transfer means housed in the first separation means, whereby all of the less volatile components from the first part are condensed at the same time. ,
  (4) The second portion is further cooled in the first heat exchange means,
  (5) the further cooled first portion and the further cooled second portion are mixed, resulting in a cooled gas stream;
  (6) The cooled gas stream is expanded to a lower pressure, thereby further cooling;
  (7) the expanded, cooled gas stream is fed as a bottom feed to an absorption means contained in a processing assembly;
  (8) The first distillate stream is collected from the lower region of the absorption means and heated in the first heat / mass transfer means, thereby supplying at least part of the cooling of step (3), The heated first distillate stream is then fed as an upper feed or an intermediate feed to the mass transfer means contained in the processing assembly,
  (9) The first distillation steam stream is collected from the upper region of the mass transfer means, and is sufficiently cooled in the second heat exchange means to condense at least a part of the first distillation steam stream,
  (10) The at least partly condensed first distillation vapor stream is fed to a second separation means and separated in the second separation means, whereby the condensed stream and the first distillation vapor stream A residual vapor stream containing all of the uncondensed vapor remaining after the is cooled,
  (11) At least a portion of the condensed stream is fed as an upper feed to the absorption means;
  (12) A second distillation vapor stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least a part of the cooling of step (9);
  (13) The heated second distillation vapor stream is mixed with all of the residual vapor stream, resulting in a mixed vapor stream;
  (14) The mixed steam stream is heated in the first heat exchange means, thereby supplying at least a part of the cooling of step (1) and step (4), and then the heated mixed steam stream Is released as the volatile residual gas fraction,
  (15) The second distillate stream is collected from the lower region of the mass transfer means and heated in the second heat / mass transfer means housed in the processing assembly, thereby removing the more volatile components. Simultaneously removing from the second distillate stream, and then releasing the heated and removed second distillate stream from the processing assembly as the relatively less volatile fraction;
  (16) The amount and temperature of the feed stream to the absorption means maintains the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively volatile fraction are recovered. Effective to do,
Method.   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ A process for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components comprising:
  (1) The gas stream is partially cooled in the first heat exchange means,
  (2) the partially cooled gas stream is divided into a first part and a second part;
  (3) The first part is further cooled in the first heat and mass transfer means accommodated in the first separation means, whereby the less volatile components from the first part are condensed at the same time,
  (4) The second portion is further cooled in the first heat exchange means,
  (5) The further cooled second part is led to the first separation means so that it is condensed as the first part is further cooled and as the second part is further cooled. All of the resulting liquid is mixed to form at least one liquid stream, and the remainder of the further cooled first portion and the further cooled second portion forms a vapor stream;
  (6) the vapor stream is expanded to a lower pressure, thereby further cooling;
  (7) the expanded, cooled vapor stream is fed as a bottom feed to an absorption means contained in a processing assembly;
  (8) the at least one liquid stream is expanded to the lower pressure;
  (9) The first distillate stream is collected from the lower region of the absorption means and heated in the first heat / mass transfer means, thereby supplying at least a part of the cooling of step (3), The heated first distillate stream is then fed as an upper feed or an intermediate feed to the mass transfer means contained in the processing assembly,
  (10) The first distillation steam stream is collected from the upper region of the mass transfer means, and is sufficiently cooled in the second heat exchange means to condense at least a part of the first distillation steam stream,
  (11) The at least partially condensed first distillation vapor stream is fed to a second separation means and separated in the second separation means, whereby the condensed stream and the first distillation vapor stream A residual vapor stream containing all of the uncondensed vapor remaining after the is cooled,
  (12) At least a portion of the condensed stream is fed as an upper feed to the absorption means;
  (13) A second distillation vapor stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least a part of the cooling of step (10);
  (14) The heated second distillation vapor stream is mixed with all of the residual vapor stream, resulting in the formation of a mixed vapor stream;
  (15) The mixed steam stream is heated in the first heat exchange means, thereby supplying at least a portion of the cooling of step (1) and step (4), and then the heated mixed steam stream Is released as the volatile residual gas fraction,
  (16) The expanded at least one liquid stream is heated in the first heat exchange means, thereby supplying at least a portion of the cooling of step (1), and then the heated, expanded At least one liquid stream is fed to the mass transfer means as a bottom feed;
  (17) The second distillate stream is collected from the lower region of the mass transfer means and heated in the second heat / mass transfer means housed in the processing assembly, thereby removing the more volatile components. Simultaneously removing from the second distillate stream, and then releasing the heated and removed second distillate stream from the processing assembly as the relatively less volatile fraction;
  (18) The amount and temperature of the feed stream to the absorption means maintains the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively volatile fraction are recovered. Effective to do,
Method.   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ A process for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components comprising:
  (1) The gas stream is partially cooled in the first heat exchange means,
  (2) the partially cooled gas stream is divided into a first part and a second part;
  (3) The first portion is further cooled in the second heat exchange means,
  (4) The second portion is further cooled in the first heat exchange means,
  (5) the further cooled first portion and the further cooled second portion are mixed, resulting in a cooled gas stream;
  (6) The cooled gas stream is expanded to a lower pressure, thereby further cooling;
  (7) the expanded, cooled gas stream is fed as a bottom feed to an absorption means contained in a processing assembly;
  (8) The first distillate stream is collected from the lower region of the absorption means and heated in the second heat exchange means, whereby at least a part of the cooling of step (3) is supplied and heated. The first distillate stream is then fed as an upper feed or an intermediate feed to the mass transfer means contained in the processing assembly;
  (9) The first distillation steam stream is collected from the upper region of the mass transfer means, and is sufficiently cooled in the third heat exchange means to condense at least a part of the first distillation steam stream,
  (10) The at least partially condensed first distillation vapor stream is fed to a separation means and separated in the separation means, whereby the condensed stream and the first distillation vapor stream are cooled. A residual vapor stream containing all of the uncondensed vapor remaining behind is formed,
  (11) At least a portion of the condensed stream is fed as an upper feed to the absorption means;
  (12) A second distillation vapor stream is collected from the upper region of the absorption means and heated in the third heat exchange means, thereby supplying at least a part of the cooling of step (9);
  (13) The heated second distillation vapor stream is mixed with all of the residual vapor stream, resulting in a mixed vapor stream;
  (14) The mixed steam stream is heated in the first heat exchange means, thereby supplying at least a part of the cooling of step (1) and step (4), and then the heated mixed steam stream Is released as the volatile residual gas fraction,
  (15) The second distillate stream is collected from the lower region of the mass transfer means and heated in the heat / mass transfer means accommodated in the processing assembly, whereby the more volatile components are removed from the first transfer stream. Simultaneously removing from the distillate stream, then discharging the heated and removed second distillate stream from the processing assembly as the relatively less volatile fraction;
  (16) The amount and temperature of the feed stream to the absorption means maintains the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively volatile fraction are recovered. Effective to do,
Method.   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ A process for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components comprising:
  (1) The gas stream is partially cooled in the first heat exchange means,
  (2) the partially cooled gas stream is divided into a first part and a second part;
  (3) The first portion is further cooled in the second heat exchange means,
  (4) The second portion is further cooled in the first heat exchange means,
  (5) the further cooled first portion and the further cooled second portion are mixed, resulting in the formation of a partially condensed gas stream;
  (6) The partially condensed gas stream is fed to a first separation means and separated in the first separation means, thereby providing a vapor stream and at least one liquid stream;
  (7) the steam stream is expanded to a lower pressure, thereby further cooling;
  (8) the expanded, cooled vapor stream is fed as a bottom feed to an absorption means contained in a processing assembly;
  (9) the at least one liquid stream is expanded to the lower pressure;
  (10) The first distillate stream is collected from the lower region of the absorption means and heated in the second heat exchange means, whereby at least part of the cooling of step (3) is supplied and heated. The first distillate stream is then fed as an upper feed or an intermediate feed to the mass transfer means contained in the processing assembly;
  (11) The first distillation steam stream is collected from the upper region of the mass transfer means, and is sufficiently cooled in the third heat exchange means, so that at least a part of the first distillation steam stream is condensed,
  (12) The at least partly condensed first distillation vapor stream is fed to a second separation means and separated in the second separation means, whereby the condensed stream and the first distillation vapor stream A residual vapor stream containing all of the uncondensed vapor remaining after the is cooled,
  (13) At least a portion of the condensed stream is fed as an upper feed to the absorption means;
  (14) A second distillation vapor stream is collected from the upper region of the absorption means and heated in the third heat exchange means, thereby supplying at least a part of the cooling of step (11);
  (15) The heated second distillation vapor stream is mixed with all of the residual vapor stream, resulting in the formation of a mixed vapor stream;
  (16) The mixed steam stream is heated in the first heat exchange means, thereby supplying at least a part of the cooling of step (1) and step (4), and then the heated mixed steam stream Is released as the volatile residual gas fraction,
  (17) The expanded at least one liquid stream is heated in the first heat exchange means, thereby supplying at least a portion of the cooling of step (1) and then the heated, expanded At least one liquid stream is fed to the mass transfer means as a bottom feed;
  (18) The second distillate stream is collected from the lower region of the mass transfer means and heated in the heat / mass transfer means housed in the processing assembly, whereby the more volatile components are removed from the first transfer stream. Simultaneously removing from the distillate stream, then discharging the heated and removed second distillate stream from the processing assembly as the relatively less volatile fraction;
  (19) The amount and temperature of the feed stream to the absorption means maintains the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively volatile fraction are recovered. Effective to do,
Method. 9. A method according to claim 2, 4, 5, 6, or 8, wherein the first separating means is housed in the processing assembly. (1) supplying the heated first distillate stream to the mass transfer means at an intermediate feed position;
(2) dividing the condensed stream into at least a first reflux stream and a second reflux stream;
(3) supplying the first reflux stream as the upper feed to the absorption means;
(4) supplying the second reflux stream to the mass transfer means as the upper feed;
The method of claim 3, 4, 5, 6, 7, or 8 .   Storing the first separating means in the processing assembly;
  (1) supplying the heated first distillate stream to the mass transfer means at an intermediate feed position;
  (2) dividing the condensed stream into at least a first reflux stream and a second reflux stream;
  (3) supplying the first reflux stream as the upper feed to the absorption means;
  (4) supplying the second reflux stream to the mass transfer means as the upper feed;
9. A method according to claim 4, 5, 6, or 8. (1) a gas collecting means is housed in the processing assembly;
(2) An additional heat / mass transfer means is included in the gas collection means, the additional heat / mass transfer means including one or more paths for an external refrigerant,
(3) the cooled gas stream is thus collected in the gas collection means, he guide to the additional heat-mass transfer means, is further cooled by the external coolant,
(4) expanding the further cooled gas stream to the lower pressure and then feeding it to the absorption means as the bottom feed;
The method of claim 1, 3 , 7 , 1 0 , or 11 . (1) An additional heat / mass transfer means is provided in the further separation means, the additional heat / mass transfer means comprising one or more paths for an external refrigerant,
(2) directing the vapor stream to the additional heat and mass transfer means and cooling with the external refrigerant to form additional condensed water;
(3) the condensed water becomes part of the at least one liquid stream separated in the further separation means;
The method of claim 2 , 4 , 8 , 9 , 1 0 , or 11 . A gas stream containing methane, C ₂ component, C ₃ component, and heavier hydrocarbon component is separated into a volatile residual gas fraction and a relatively large volume containing the majority of the C ₃ component and heavier hydrocarbon component. An apparatus for splitting into fractions of low volatility,
(1) first heat exchange means for cooling the gas stream;
(2) expansion means connected to the first heat exchange means for receiving the cooled gas stream and expanding the cooled gas stream to a lower pressure;
(3) the absorbent means contained in a processing assembly and connected to the expansion means for receiving the expanded and cooled gas stream as a bottom feed to the absorption means;
(4) first liquid collection means contained in the processing assembly and connected to the absorption means for receiving a first distillate stream from a region below the absorption means;
(5) the mass transfer means contained in the processing assembly and connected to the first liquid collection means for receiving the first distillate stream as an upper feed to the mass transfer means;
(6) and from said upper region of the mass transfer means for receiving a first distillation vapor stream, the first steam collecting means connected to said accommodated in the processing assembly and the mass transfer means,
(7) receiving the first distillation vapor stream, connected to the first vapor collection means for sufficiently cooling the first distillation vapor stream and condensing at least a portion of the first distillation vapor stream; Second heat exchange means,
(8) receiving the at least partially condensed first distillation steam stream, cooling the at least partially condensed first distillation steam stream, the condensed stream, and the first distillation steam stream; Separating means connected to the second heat exchange means for separating into a residual steam stream containing all of the uncondensed steam remaining after
(9) the absorbing means further connected to the separating means for receiving at least a portion of the condensed stream as an upper feed to the absorbing means;
(10) a second vapor collection means contained in the processing assembly and connected to the absorption means for receiving a second distillation vapor stream from an upper region of the absorption means;
(11) The second heat further connected to the second steam collecting means for receiving and heating the second distillation steam stream to supply at least a portion of the cooling of the step (7). Exchange means,
(12) Mixing means connected to the second heat exchange means and the separation means for receiving the heated second distillation steam stream and all of the residual steam stream to form a mixed steam stream When,
(13) receiving and heating the mixed vapor stream to supply at least a portion of the cooling of step (1) and then releasing the heated mixed vapor stream as the volatile residual gas fraction The first heat exchange means further connected to the mixing means for
(14) and a second liquid collection means connected to a second distillate stream for receiving the lower region of the mass transfer means, housed in said processing assembly and said mass transfer means,
(15) receiving and heating the second distillate stream to simultaneously remove the more volatile components from the second distillate stream, and then removing the heated and removed second distillate stream; A heat and mass transfer means contained in the processing assembly and connected to the second liquid collecting means for releasing the relatively low volatile fraction from the processing assembly;
(16) the amount of the feed stream to the absorption means for maintaining the temperature in the upper region of the absorption means at a temperature at which the majority of the components of the relatively low volatility are recovered And control means configured to adjust the temperature.   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ An apparatus for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components,
  (1) first heat exchange means for partially condensing the gas stream by sufficiently cooling the gas stream;
  (2) in the first heat exchange means for receiving the partially condensed gas stream and separating the partially condensed gas stream into a vapor stream and at least one liquid stream; Connected first separating means;
  (3) first expansion means connected to the first separation means for further cooling the vapor stream by receiving the vapor stream and expanding the vapor stream to a lower pressure;
  (4) the absorbent means contained in a processing assembly and connected to the first expansion means for receiving the expanded cooled vapor stream as a bottom feed to the absorption means;
  (5) a second expansion means connected to the first separation means for receiving the at least one liquid stream and expanding the at least one liquid stream to the lower pressure;
  (6) first liquid collection means contained in the processing assembly and connected to the absorption means for receiving a first distillate stream from a region below the absorption means;
  (7) the mass transfer means contained in the processing assembly and connected to the first liquid collection means for receiving the first distillate stream as an upper feed to the mass transfer means;
  (8) a first vapor collection means contained in the processing assembly and connected to the mass transfer means for receiving a first distillation vapor stream from an upper region of the mass transfer means;
  (9) receiving the first distillation steam stream, connected to the first steam collecting means for sufficiently cooling the first distillation steam stream and condensing at least a part of the first distillation steam stream; Second heat exchange means,
  (10) receiving the at least partially condensed first distillation steam stream, cooling the at least partially condensed first distillation steam stream, the condensed stream, and the first distillation steam stream; Second separation means connected to the second heat exchange means for separating into a residual steam stream containing all of the uncondensed steam remaining after
  (11) the absorbing means further connected to the second separating means for receiving at least a portion of the condensed stream as an upper feed to the absorbing means;
  (12) second vapor collection means contained in the processing assembly and connected to the absorption means for receiving a second distillation vapor stream from an upper region of the absorption means;
  (13) The second heat exchange further connected to the second steam collecting means for supplying at least a portion of the cooling of step (9) by receiving and heating the second distilled steam stream Means,
  (14) connected to the second heat exchange means and the second separation means for receiving the heated second distillation steam stream and all of the residual steam stream to form a mixed steam stream Mixing means;
  (15) receiving and heating the mixed vapor stream to supply at least a portion of the cooling of step (1) and then releasing the heated mixed vapor stream as the volatile residual gas fraction The first heat exchange means further connected to the mixing means for
  (16) receiving and heating the expanded at least one liquid stream to supply at least a portion of the cooling of step (1), wherein the first heat exchange means is further connected to the mass transfer means; And as a result, the heated expanded at least one liquid stream is supplied as a bottom feed to the first heat exchange means, the first heat exchange means connected to the second expansion means;
  (17) a second liquid collection means contained in the processing assembly and connected to the mass transfer means for receiving a second distillate stream from a lower region of the mass transfer means;
  (18) removing the more volatile components from the second distillate stream simultaneously by receiving and heating the second distillate stream, and then removing the heated and removed second distillate stream; A heat and mass transfer means contained in the processing assembly and connected to the second liquid collecting means for discharging from the processing assembly as the relatively low volatility fraction;
  (19) The amount of the feed stream to the absorption means in order to maintain the temperature of the upper region of the absorption means at a temperature at which most of the components of the relatively low volatility are recovered And control means configured to adjust the temperature;
A device comprising:   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ An apparatus for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components,
  (1) first heat exchange means for cooling the gas stream;
  (2) expansion means connected to the first heat exchange means for receiving the cooled gas stream and expanding the cooled gas stream to a lower pressure;
  (3) the absorption means contained in a processing assembly and connected to the expansion means for receiving the expanded cooled gas stream as a bottom feed to the absorption means;
  (4) first liquid collection means contained in the processing assembly and connected to the absorption means for receiving a first distillate stream from a region below the absorption means;
  (5) second heat exchange means connected to the first liquid collection means for receiving and heating the first distillate stream;
  (6) The mass transfer contained in the processing assembly and connected to the second heat exchange means for receiving the heated first distillate stream as an upper feed or intermediate feed to the mass transfer means Means,
  (7) first vapor collection means contained in the processing assembly and connected to the mass transfer means for receiving a first distillation vapor stream from an upper region of the mass transfer means;
  (8) receiving at least the first distillation steam stream, sufficiently cooling the first distillation steam stream to condense at least a portion of the first distillation steam stream, so that at least the cooling of step (5) The second heat exchange means further connected to the first steam collecting means for supplying a portion;
  (9) receiving the at least partially condensed first distillation steam stream, cooling the at least partially condensed first distillation steam stream, the condensed stream, and the first distillation steam stream being cooled; Separating means connected to the second heat exchange means for separating into a residual steam stream containing all of the uncondensed steam remaining after
  (10) the absorbing means further connected to the separating means for receiving at least a portion of the condensed stream as an upper feed to the absorbing means;
  (11) second vapor collection means contained in the processing assembly and connected to the absorption means for receiving a second distillation vapor stream from an upper region of the absorption means;
  (12) The second heat exchange further connected to the second steam collection means for supplying at least a portion of the cooling of step (8) by receiving and heating the second distillation steam stream Means,
  (13) Mixing means connected to the second heat exchange means and the separation means for receiving the heated second distillation steam stream and all of the residual steam stream to form a mixed steam stream When,
  (14) receiving and heating the mixed vapor stream to supply at least a portion of the cooling of step (1) and then releasing the heated mixed vapor stream as the volatile residual gas fraction The first heat exchange means further connected to the mixing means for
  (15) second liquid collection means contained in the processing assembly and connected to the mass transfer means for receiving a second distillate stream from a lower region of the mass transfer means;
  (16) receiving and heating the second distillate stream to simultaneously remove the more volatile components from the second distillate stream and then removing the heated and removed second distillate stream; A heat and mass transfer means contained in the processing assembly and connected to the second liquid collecting means for discharging from the processing assembly as the relatively low volatility fraction;
  (17) The amount of the feed stream to the absorption means for maintaining the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively low volatility are recovered And control means configured to adjust the temperature;
A device comprising:   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ An apparatus for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components,
  (1) first heat exchange means for partially condensing the gas stream by sufficiently cooling the gas stream;
  (2) in the first heat exchange means for receiving the partially condensed gas stream and separating the partially condensed gas stream into a vapor stream and at least one liquid stream; Connected first separating means;
  (3) first expansion means connected to the first separation means for further cooling the vapor stream by receiving the vapor stream and expanding the vapor stream to a lower pressure;
  (4) the absorbent means contained in a processing assembly and connected to the first expansion means for receiving the expanded cooled vapor stream as a bottom feed to the absorption means;
  (5) a second expansion means connected to the first separation means for receiving the at least one liquid stream and expanding the at least one liquid stream to a lower pressure;
  (6) first liquid collection means contained in the processing assembly and connected to the absorption means for receiving a first distillate stream from a region below the absorption means;
  (7) second heat exchange means connected to the first liquid collection means for receiving and heating the first distillate stream;
  (8) The mass transfer contained in the processing assembly and connected to the second heat exchange means for receiving the heated first distillate stream as an upper feed or intermediate feed to the mass transfer means Means,
  (9) first vapor collection means contained in the processing assembly and connected to the mass transfer means for receiving a first distillation vapor stream from an upper region of the mass transfer means;
  (10) receiving at least the first distillation steam stream, sufficiently cooling the first distillation steam stream to condense at least a portion of the first distillation steam stream, thereby at least the heating of step (7); The second heat exchange means further connected to the first steam collecting means for supplying a portion;
  (11) receiving the at least partially condensed first distillation steam stream, cooling the at least partially condensed first distillation steam stream, the condensed stream, and the first distillation steam stream; Second separation means connected to the second heat exchange means for separating into a residual steam stream containing all of the uncondensed steam remaining after
  (12) the absorbing means further connected to the second separating means for receiving at least a portion of the condensed stream as an upper feed to the absorbing means;
  (13) second vapor collection means contained in the processing assembly and connected to the absorption means for receiving a second distillation vapor stream from an upper region of the absorption means;
  (14) The second heat exchange further connected to the second steam collection means for supplying at least a portion of the cooling of step (10) by receiving and heating the second distillation steam stream Means,
  (15) connected to the second heat exchange means and the second separation means for receiving the heated second distillation steam stream and all of the residual steam stream to form a mixed steam stream; Mixing means;
  (16) supplying and heating the mixed vapor stream to supply at least a portion of the cooling of step (1) and then releasing the heated mixed vapor stream as the volatile residual gas fraction The first heat exchange means further connected to the mixing means for
  (17) receiving and heating the expanded at least one liquid stream to supply at least a portion of the cooling of step (1), wherein the first heat exchange means is further connected to the mass transfer means; And, as a result, the heated expanded at least one liquid stream is supplied as a bottom feed to the first heat exchange means, the first heat exchange means further connected to the second expansion means; ,
  (18) second liquid collection means contained in the processing assembly and connected to the mass transfer means for receiving a second distillate stream from a lower region of the mass transfer means;
  (19) receiving and heating the second distillate stream to simultaneously remove the more volatile components from the second distillate stream and then removing the heated and removed second distillate stream; A heat and mass transfer means contained in the processing assembly and connected to the second liquid collecting means for discharging from the processing assembly as the relatively low volatility fraction;
  (20) the amount of the feed stream to the absorption means for maintaining the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively low volatility are recovered. And control means configured to adjust the temperature;
A device comprising:   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ An apparatus for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components,
  (1) first heat exchange means for partially cooling the gas stream;
  (2) a split connected to the first heat exchange means for receiving the partially cooled gas stream and splitting the partially cooled gas stream into a first part and a second part; Means,
  (3) Receiving and further cooling the first part to accommodate all of the less volatile components from the first part at the same time and contained in the first separation means and the split First heat and mass transfer means connected to the means;
  (4) the first heat exchange means further connected to the dividing means for receiving and further cooling the second portion;
  (5) The first heat / mass transfer means and the first heat exchange means for receiving the further cooled first part and the further cooled second part to form a cooled gas stream. First mixing means connected to
  (6) expansion means connected to the first mixing means for receiving the cooled gas stream and expanding the cooled gas stream to a lower pressure;
  (7) the absorbing means contained in a processing assembly and connected to the expansion means for receiving the expanded cooled gas stream as a bottom feed to the absorption means;
  (8) a first liquid collecting means contained in the processing assembly and connected to the absorbing means for receiving a first distillate stream from a region below the absorbing means;
  (9) receiving the first distillate stream and heating the first heat stream further connected to the first liquid collecting means for providing at least part of the cooling of step (3); Mass transfer means;
  (10) receiving said heated first distillate stream as an upper feed or intermediate feed to the mass transfer means and contained in said processing assembly and connected to said first heat and mass transfer means Mass transfer means;
  (11) first vapor collection means contained in the processing assembly and connected to the mass transfer means for receiving a first distillation vapor stream from an upper region of the mass transfer means;
  (12) receiving the first distillation steam stream, connected to the first steam collecting means for sufficiently cooling the first distillation steam stream and condensing at least a part of the first distillation steam stream; Second heat exchange means,
  (13) receiving the at least partially condensed first distillation steam stream, cooling the at least partially condensed first distillation steam stream, the condensed stream, and the first distillation steam stream; Second separation means connected to the second heat exchange means for separating into a residual steam stream containing all of the uncondensed steam remaining after
  (14) the absorbing means further connected to the second separating means for receiving at least a portion of the condensed stream as an upper feed to the absorbing means;
  (15) a second vapor collection means contained in the processing assembly and connected to the absorption means for receiving a second distilled vapor stream from an upper region of the absorption means;
  (16) The second heat exchange further connected to the second steam collection means for supplying at least a portion of the cooling of step (12) by receiving and heating the second distillation steam stream Means,
  (17) connected to the second heat exchange means and the second separation means for receiving the heated second distillation steam stream and all of the residual steam stream to form a mixed steam stream; A second mixing means;
  (18) providing and heating at least a portion of the cooling of step (1) and step (4) by receiving and heating the mixed vapor stream, and then the heated mixed vapor stream is converted to the volatile residue; The first heat exchange means further connected to the second mixing means for releasing as a gas fraction;
  (19) Second liquid collection means contained in the processing assembly and connected to the mass transfer means for receiving a second distillate stream from a lower region of the mass transfer means;
  (20) receiving and heating the second distillate stream to simultaneously remove the more volatile components from the second distillate stream, and then removing the heated and removed second distillate stream; A second heat and mass transfer means contained in the processing assembly and connected to the second liquid collecting means for discharging from the processing assembly as the relatively low volatility fraction;
  (21) the amount of the feed stream to the absorption means for maintaining the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively low volatility are recovered And control means configured to adjust the temperature;
A device comprising:   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ An apparatus for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components,
  (1) first heat exchange means for partially cooling the gas stream;
  (2) a split connected to the first heat exchange means for receiving the partially cooled gas stream and splitting the partially cooled gas stream into a first part and a second part; Means,
  (3) Receiving the first part and further cooling it to accommodate the less volatile components from the first part at the same time and accommodated in the first separating means and the dividing means First heat and mass transfer means connected to
  (4) the first heat exchange means further connected to the dividing means for receiving and further cooling the second portion;
  (5) By receiving the further cooled second portion, all of the condensed liquid is mixed as the first portion is further cooled and as the second portion is further cooled. At least one liquid stream is formed, and the further cooled first portion and the remainder of the further cooled second portion are further connected to the first heat exchange means, which will form a vapor stream. Said first separating means;
  (6) first expansion means connected to the first separation means for further cooling the vapor stream by receiving the vapor stream and expanding the vapor stream to a lower pressure;
  (7) the absorbent means contained in a processing assembly and connected to the first expansion means for receiving the expanded cooled vapor stream as a bottom feed to the absorption means;
  (8) second expansion means connected to the first separation means for receiving the at least one liquid stream and expanding the at least one liquid stream to a lower pressure;
  (9) a first liquid collecting means contained in the processing assembly and connected to the absorbing means for receiving a first distillate stream from a region below the absorbing means;
  (10) receiving the first distillate stream and heating the first heat stream further connected to the first liquid collecting means for providing at least part of the cooling of step (3); Mass transfer means;
  (11) receiving the heated first distillate stream as an upper feed or intermediate feed to the mass transfer means and contained in the processing assembly and connected to the first heat and mass transfer means Mass transfer means;
  (12) first vapor collection means contained in the processing assembly and connected to the mass transfer means for receiving a first distillation vapor stream from an upper region of the mass transfer means;
  (13) receiving the first distillation steam stream, connected to the first steam collecting means for sufficiently cooling the first distillation steam stream and condensing at least a part of the first distillation steam stream; Second heat exchange means,
  (14) receiving the at least partially condensed first distillation vapor stream, cooling the at least partially condensed first distillation vapor stream, the condensed stream, and the first distillation vapor stream; Second separation means connected to the second heat exchange means for separating into a residual steam stream containing all of the uncondensed steam remaining after
  (15) the absorbing means further connected to the second separating means for receiving at least a portion of the condensed stream as an upper feed to the absorbing means;
  (16) second vapor collection means contained in the processing assembly and connected to the absorption means for receiving a second distilled vapor stream from an upper region of the absorption means;
  (17) The second heat exchange further connected to the second steam collection means for supplying at least a portion of the cooling of step (13) by receiving and heating the second distillation steam stream Means,
  (18) connected to the second heat exchange means and the second separation means for receiving the heated second distillation steam stream and all of the residual steam stream to form a mixed steam stream Mixing means;
  (19) providing and heating at least a portion of the cooling of step (1) and step (4) by receiving and heating the mixed vapor stream, and then heating the heated mixed vapor stream to the volatile residue; The first heat exchange means further connected to the mixing means for releasing as a gas fraction;
  (20) receiving and heating the expanded at least one liquid stream to supply at least a portion of the cooling of step (1), wherein the first heat exchange means is further connected to the mass transfer means; And, as a result, the heated expanded at least one liquid stream is supplied as a bottom feed to the first heat exchange means, the first heat exchange means further connected to the second expansion means; ,
  (21) second liquid collection means contained in the processing assembly and connected to the mass transfer means for receiving a second distillate stream from a lower region of the mass transfer means;
  (22) receiving and heating the second distillate stream to simultaneously remove the more volatile components from the second distillate stream, and then removing the heated and removed second distillate stream; A second heat and mass transfer means contained in the processing assembly and connected to the second liquid collecting means for discharging from the processing assembly as the relatively low volatility fraction;
  (23) the amount of the feed stream to the absorption means for maintaining the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively low volatility are recovered And control means configured to adjust the temperature;
A device comprising:   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ An apparatus for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components,
  (1) first heat exchange means for partially cooling the gas stream;
  (2) a split connected to the first heat exchange means for receiving the partially cooled gas stream and splitting the partially cooled gas stream into a first part and a second part; Means,
  (3) a second heat exchange means connected to the dividing means for receiving and further cooling the first portion;
  (4) the first heat exchange means further connected to the dividing means for receiving and further cooling the second portion;
  (5) connected to the second heat exchange means and the first heat exchange means for receiving the further cooled first portion and the further cooled second portion to form a cooled gas stream; First mixing means,
  (6) expansion means connected to the first mixing means for receiving the cooled gas stream and expanding the cooled gas stream to a lower pressure;
  (7) the absorbing means contained in a processing assembly and connected to the expansion means for receiving the expanded cooled gas stream as a bottom feed to the absorption means;
  (8) a first liquid collecting means contained in the processing assembly and connected to the absorbing means for receiving a first distillate stream from a region below the absorbing means;
  (9) receiving the first distillate stream and heating the second distillate further connected to the first liquid collection means for providing at least a portion of the cooling of step (3); Mass transfer means;
  (10) The mass transfer contained in the processing assembly and connected to the second heat exchange means for receiving the heated first distillate stream as an upper feed or intermediate feed to the mass transfer means Means,
  (11) first vapor collection means contained in the processing assembly and connected to the mass transfer means for receiving a first distillation vapor stream from an upper region of the mass transfer means;
  (12) receiving the first distillation steam stream, connected to the first steam collecting means for sufficiently cooling the first distillation steam stream and condensing at least a part of the first distillation steam stream; A third heat exchange means,
  (13) receiving the at least partially condensed first distillation steam stream, cooling the at least partially condensed first distillation steam stream, the condensed stream, and the first distillation steam stream; Separating means connected to the third heat exchange means for separating into a residual steam stream containing all of the uncondensed steam remaining after
  (14) the absorbing means further connected to the separating means for receiving at least a portion of the condensed stream as an upper feed to the absorbing means;
  (15) a second vapor collection means contained in the processing assembly and connected to the absorption means for receiving a second distilled vapor stream from an upper region of the absorption means;
  (16) The third heat exchange further connected to the second steam collection means for supplying at least a portion of the cooling of step (12) by receiving and heating the second distillation steam stream Means,
  (17) a second connected to the third heat exchange means and the separation means for receiving the heated second distillation steam stream and all of the residual steam stream to form a mixed steam stream; Mixing means;
  (18) providing and heating at least a portion of the cooling of step (1) and step (4) by receiving and heating the mixed vapor stream, and then the heated mixed vapor stream is converted to the volatile residue; The first heat exchange means further connected to the second mixing means for releasing as a gas fraction;
  (19) Second liquid collection means contained in the processing assembly and connected to the mass transfer means for receiving a second distillate stream from a lower region of the mass transfer means;
  (20) receiving and heating the second distillate stream to simultaneously remove the more volatile components from the second distillate stream, and then removing the heated and removed second distillate stream; A heat and mass transfer means contained in the processing assembly and connected to the second liquid collecting means for discharging from the processing assembly as the relatively low volatility fraction;
  (21) the amount of the feed stream to the absorption means for maintaining the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively low volatility are recovered And control means configured to adjust the temperature;
A device comprising:   Methane, C ₂ Ingredient C ₃ A gas stream containing the components and heavier hydrocarbon components, a volatile residual gas fraction, and said C ₃ An apparatus for splitting into a relatively less volatile fraction containing a majority of the components and heavier hydrocarbon components,
  (1) first heat exchange means for partially cooling the gas stream;
  (2) a split connected to the first heat exchange means for receiving the partially cooled gas stream and splitting the partially cooled gas stream into a first part and a second part; Means,
  (3) a second heat exchange means connected to the dividing means for receiving and further cooling the first portion;
  (4) the first heat exchange means further connected to the dividing means for receiving and further cooling the second portion;
  (5) the second heat exchange means and the first heat exchange for receiving the further cooled first portion and the further cooled second portion to form a partially condensed gas stream; First mixing means connected to the means;
  (6) connected to the first mixing means for receiving the partially condensed gas stream and separating the partially condensed gas stream into a vapor stream and at least one liquid stream; First separating means,
  (7) first expansion means connected to the first separation means for further cooling the vapor stream by receiving the vapor stream and expanding the vapor stream to a lower pressure;
  (8) the absorbent means contained in a processing assembly and connected to the first expansion means for receiving the expanded cooled vapor stream as a bottom feed to the absorption means;
  (9) a second expansion means connected to the first separation means for receiving the at least one liquid stream and expanding the at least one liquid stream to a lower pressure;
  (10) first liquid collection means received in the processing assembly and connected to the absorption means for receiving a first distillate stream from a region below the absorption means;
  (11) receiving the first distillate stream and heating the second distillate further connected to the first liquid collecting means for providing at least part of the cooling of step (3); Mass transfer means;
  (12) The mass transfer contained in the processing assembly and connected to the second heat exchange means for receiving the heated first distillate stream as an upper feed or intermediate feed to the mass transfer means Means,
  (13) first vapor collection means contained in the processing assembly and connected to the mass transfer means for receiving a first distillation vapor stream from an upper region of the mass transfer means;
  (14) connected to the first steam collecting means for receiving the first distilled steam stream, sufficiently cooling the first distilled steam stream, and condensing at least a part of the first distilled steam stream; A third heat exchange means,
  (15) receiving the at least partially condensed first distillation vapor stream, cooling the at least partially condensed first distillation vapor stream, the condensed stream and the first distillation vapor stream; Second separation means connected to the third heat exchange means for separating into a residual steam stream containing all of the uncondensed steam remaining after
  (16) the absorbing means further connected to the second separating means for receiving at least a portion of the condensed stream as an upper feed to the absorbing means;
  (17) second vapor collection means contained in the processing assembly and connected to the absorption means for receiving a second distilled vapor stream from an upper region of the absorption means;
  (18) The third heat exchange further connected to the second steam collection means for supplying at least a portion of the cooling of step (14) by receiving and heating the second distillation steam stream Means,
  (19) connected to the third heat exchange means and the second separation means for receiving the heated second distillation steam stream and all of the residual steam stream to form a mixed steam stream A second mixing means;
  (20) providing and heating at least a portion of the cooling of step (1) and step (4) by receiving and heating the mixed vapor stream, and then supplying the heated mixed vapor stream to the volatile residue; The first heat exchange means further connected to the second mixing means for releasing as a gas fraction;
  (21) receiving and heating the expanded at least one liquid stream to supply at least a portion of the cooling of step (1), wherein the first heat exchange means is further connected to the mass transfer means; And, as a result, the heated expanded at least one liquid stream is supplied as a bottom feed to the first heat exchange means, the first heat exchange means further connected to the second expansion means; ,
  (22) second liquid collection means contained in the processing assembly and connected to the mass transfer means for receiving a second distillate stream from a lower region of the mass transfer means;
  (23) receiving and heating the second distillate stream to simultaneously remove the more volatile components from the second distillate stream, and then removing the heated and removed second distillate stream; A heat and mass transfer means contained in the processing assembly and connected to the second liquid collecting means for discharging from the processing assembly as the relatively low volatility fraction;
  (24) The amount of the feed stream to the absorption means for maintaining the temperature in the upper region of the absorption means at a temperature at which most of the components of the relatively low volatility are recovered. And control means configured to adjust the temperature;
A device comprising: Said first separating means, accommodated in said processing assembly, apparatus according to claim 15, 17, 18, 19 or 21,. (1) The mass transfer means is connected to the second heat exchange means and configured to receive the heated first distillate stream at an intermediate feed position;
(2) connecting a dividing means to the separating means, receiving the condensed stream and dividing it into at least a first reflux stream and a second reflux stream;
(3) the absorbing means is connected to the dividing means and configured to receive the first reflux stream as the upper feed;
(4) The mass transfer means is connected to the dividing means and configured to receive the second reflux stream as the upper feed.
The apparatus according to claim 16 or 17 . (1) The mass transfer means is connected to the third heat exchange means and configured to receive the heated first distillate stream at an intermediate feed position;
(2) An additional dividing means is connected to the separating means, receives the condensed stream, and divides into at least a first reflux stream and a second reflux stream;
(3) The absorbing means is connected to the additional dividing means and configured to receive the first reflux stream as the upper feed;
(4) The mass transfer means is connected to the additional dividing means and configured to receive the second reflux stream as the upper feed.
The apparatus according to claim 20 or 21 . (1) the mass transfer means, the connecting to a further heat-mass transfer means, configured to receive a first distillate stream the heating in the intermediate feed position,
(2) An additional dividing means is connected to the separating means, receives the condensed stream, and divides into at least a first reflux stream and a second reflux stream;
(3) The absorbing means is connected to the additional dividing means and configured to receive the first reflux stream as the upper feed;
(4) The mass transfer means is connected to the additional dividing means and configured to receive the second reflux stream as the upper feed.
The apparatus according to claim 18 or 19 .   Storing the first separating means in the processing assembly;
  (1) The mass transfer means is connected to the second heat exchange means and configured to receive the heated first distillate stream at an intermediate feed position;
  (2) connecting a dividing means to the separating means, receiving the condensed stream and dividing it into at least a first reflux stream and a second reflux stream;
  (3) the absorbing means is connected to the dividing means and configured to receive the first reflux stream as the upper feed;
  (4) The mass transfer means is connected to the dividing means and configured to receive the second reflux stream as the upper feed.
The apparatus according to claim 17, 18, 19 or 21.   Storing the first separating means in the processing assembly;
  (1) The mass transfer means is connected to the third heat exchange means and configured to receive the heated first distillate stream at an intermediate feed position;
   (2) An additional dividing means is connected to the separating means, receives the condensed stream, and divides into at least a first reflux stream and a second reflux stream;
  (3) The absorbing means is connected to the additional dividing means and configured to receive the first reflux stream as the upper feed;
  (4) The mass transfer means is connected to the additional dividing means and configured to receive the second reflux stream as the upper feed.
The apparatus according to claim 17, 18, 19 or 21.   Storing the first separating means in the processing assembly;
  (1) The mass transfer means is connected to the further heat and mass transfer means and is configured to receive the heated first distillate stream at an intermediate feed position;
  (2) An additional dividing means is connected to the separating means, receives the condensed stream, and divides into at least a first reflux stream and a second reflux stream;
  (3) The absorbing means is connected to the additional dividing means and configured to receive the first reflux stream as the upper feed;
  (4) The mass transfer means is connected to the additional dividing means and configured to receive the second reflux stream as the upper feed.
The apparatus according to claim 17, 18, 19 or 21. (1) a gas collecting means is housed in the processing assembly;
(2) An additional heat / mass transfer means is included in the gas collection means, and the additional heat / mass transfer means includes one or more paths for an external refrigerant,
(3) The gas collection means is connected to the first heat exchange means, receives the cooled gas stream, leads to the additional heat / mass transfer means, and further cools by the external refrigerant,
(4) The expansion means is connected to the gas collection means and receives the further cooled gas stream and expands to the lower pressure, and the expansion means is further connected to the absorption means and expands. Supplying a further cooled gas stream as the bottom feed,
27. The apparatus of claim 14 , 16 , 23, or 26 . (1) a gas collecting means is housed in the processing assembly;
(2) An additional heat / mass transfer means is included in the gas collection means, and the additional heat / mass transfer means includes one or more paths for an external refrigerant,
(3) the gas collecting means is connected to the further merging means, receives the cooled gas stream, leads to the additional heat and mass transfer means, and is further cooled by the external refrigerant;
(4) the expansion means, connected to said gas collection means, said further receiving the cooled gas stream, the more inflated to a low pressure, the expansion means is further connected to said absorbing means, said bottom feed Supplying the expanded and further cooled gas stream,
28. Apparatus according to claim 20, 24 or 27 . (1) An additional heat / mass transfer means is provided inside the further separation means, and the additional heat / mass transfer means comprises one or more paths for an external refrigerant,
(2) directing the vapor stream to the additional heat and mass transfer means and cooling with the external refrigerant to form an additional condensate;
(3) the condensate becomes part of the at least one liquid stream separated therein;
30. The apparatus of claim 15 , 17 , 21 , 22 , 24 , 25, 27, or 28 .