JP2013524149A - Hydrocarbon gas treatment - Google Patents

Abstract

Disclosed is a method and apparatus for a compact processor for recovering propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The gas stream is cooled, expanded to a lower pressure and fed to the absorption means. The first distillate stream emanating from the absorption means is supplied to the mass transfer means. When cooled, the first distillation vapor stream emanating from the mass transfer means is partially condensed to form a residual vapor stream and a condensed stream. The agglomerated stream is fed as an upper feed to the absorption means. The second distillation vapor stream emanating from the absorption means is heated by cooling the first distillation vapor stream, mixed with the residual vapor stream, and heated by cooling the gas stream. The second distillate stream emanating from the substance transfer means is heated in the heat / substance transfer means, and its volatile components are removed.
[Selection] Figure 21

Description

  Propylene, propane, and / or heavier hydrocarbons such as natural gas, refinery gas, and synthesis gas streams derived from other hydrocarbon materials such as coal, crude oil, naphtha, oil shale, tar sand, lignite It is possible to recover from various gases. Natural gas generally has a major portion consisting of methane and ethane. That is, the combined methane and ethane will contain at least 50 mole percent of natural gas. Natural gas contains relatively small amounts of heavy hydrocarbons such as propane, butane and pentane in addition to hydrogen, nitrogen, carbon dioxide, and other gases.

The present invention relates generally to the recovery of propylene, propane, and heavy hydrocarbons from such gas streams. Analysis of gas streams treated according to the present invention generally results in approximately 88.4% methane, 6.2% ethane and other C ₂ components, 2.6% propane and other C _{3 in} approximately mole percent. The ingredients are 0.3% isobutane, 0.6% normal butane, and 0.8% pentane, the remainder being nitrogen and carbon dioxide. Sulfur containing gases may be present.

  Historical periodic fluctuations in prices in both natural gas and its liquefied natural gas (NGL) components can sometimes reduce the increase in the value of propane, propylene, and heavier components as liquid products. there were. As a result, there has been a demand for processes for more effective recovery of these products and a process for providing effective recovery with lower capital investment. Processes available to separate these materials include processes based on gas, oil absorption, cooling of frozen oil absorption and refrigeration. In addition, cryogenic processing has become widespread due to the availability of economical facilities that generate power while simultaneously expanding and extracting heat from the gas being treated. Depending on the pressure of the gas source, the richness of the gas (ethane, ethylene, and heavy hydrocarbon components) and the desired end product, each of these processes or a combination of these processes may be used.

The cryogenic expansion process is currently generally preferred for liquefied natural gas recovery due to maximal simplification with easy start-up, operational flexibility, good efficiency, safety, and good reliability. U.S. Patent 3,292,380, U.S. Patent 4,061,481, U.S. Patent 4,140,504, U.S. Patent 4,157,904, U.S. Patent 4,171,964, U.S. Patent No. 4,185,978, U.S. Patent No. 4,251,249, U.S. Patent No. 4,278,457, U.S. Patent No. 4,519,824, U.S. Patent No. 4,617,039, U.S. Patent No. 4,687,499, U.S. Patent No. 4,689,063, U.S. Patent No. 4,690,702, U.S. Patent No. 4,854,955, U.S. Patent No. 4,869,740, U.S. Patent No. 4,889,545, U.S. Patent No. 5,275,005, U.S. Patent No. 5,555,748, U.S. Patent No. 5,566,554, U.S. Patent No. 5,568,737, US Pat. No. 5,771,71 , U.S. Patent No. 5,799,507, U.S. Patent No. 5,881,569, U.S. Patent No. 5,890,378, U.S. Patent No. 5,983,664, U.S. Patent No. 6,182,469. US Pat. No. 6,578,379, US Pat. No. 6,712,880, US Pat. No. 6,915,662, US Pat. No. 7,191,617, US Pat. No. 7,219,513 US Reissued Patent No. 33,408, copending application No. 11 / 430,412, copending application No. 11 / 839,693, copending application No. 11 / 971,491, copending application No. 12 / 206,230, co-pending application 12 / 689,616, co-pending application 12 / 717,394, co-pending application 12/7
50,862, co-pending application 12 / 772,472, co-pending application 12 / 781,259, co-pending application 12 / 868,993, co-pending application 12 / 869,007, simultaneous Pending application 12 / 869,139, co-pending application 12 / 979,563, and co-pending application 13 / 048,315 describe the associated processing (although the invention in some cases) Is based on processing conditions different from those of the cited US patents).

In a typical cryogenic expansion recovery process, the pressurized feed gas stream is cooled by heat exchange with other streams in the cryogenic expansion recovery process and / or an external refrigeration source such as a propane compression refrigeration system. As the gas cools, the liquid is condensed and collected in one or more separators as a high pressure liquid containing some of the desired C ₃ + components. Depending on the richness of the gas and the amount of liquid formed, the high pressure liquid can be expanded to a lower pressure and rectified. As a result of the evaporation that occurs while the liquid expands, the stream is further cooled. Under some circumstances, it may be desirable to precool the high pressure liquid prior to expansion to further reduce the temperature due to expansion. The expanded stream containing the liquid and gas mixture is rectified in a distillation (deethanizing) column. In the column, the expanded cooling stream (s) are distilled, resulting in residual methane, C ₂ component, nitrogen as top vapor from C ₃ component and heavier hydrocarbon components as bottom liquid product. , And other volatile gases are separated.

If the feed gas is not fully condensed (generally not necessarily fully condensed), the vapor remaining from the partial condensation is passed through an operational expander or an operational expansion engine or expansion valve, so that Lower pressure. Note that at this lower pressure, the liquid is further condensed as a result of further cooling of the stream. Expanded stream is then contacted with cold liquid entering the absorption zone in the column, as a result, absorbs C ₃ components and heavier components from the vapor portion of the expanded stream. The liquid from the absorption zone is then directed to the deethanization zone in the column.

The distillate vapor stream is withdrawn from the upper region of the deethanizing zone and 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. When the vapor portion of the cooled distillate vapor stream (if present) and the top vapor from the absorption zone mix, residual methane and C ₂ component product gas are formed.

Separation performed in this process (residual gas exiting the process that contains substantially all of the methane and C ₂ components in the feed gas and substantially no C ₃ and heavier hydrocarbon components, and C ₃ Producing a bottom fraction exiting the deethanizer comprising substantially all of the components and heavier hydrocarbon components and substantially no methane and C ₂ components or more volatile components) Consumes energy for feed gas cooling, deethanization zone reboiling, absorption zone reflux, and / or residual gas recompression.

U.S. Pat. No. 3,292,380 U.S. Pat. No. 4,061,481 U.S. Pat. No. 4,140,504 U.S. Pat. No. 4,157,904 US Pat. No. 4,171,964 US Pat. No. 4,185,978 US Pat. No. 4,251,249 U.S. Pat. No. 4,278,457 U.S. Pat. No. 4,519,824 U.S. Pat. No. 4,617,039 U.S. Pat. No. 4,687,499 US Pat. No. 4,689,063 U.S. Pat. No. 4,690,702 US Pat. No. 4,854,955 U.S. Pat. No. 4,869,740 U.S. Pat. No. 4,889,545 US Pat. No. 5,275,005 US Pat. No. 5,555,748 US Pat. No. 5,566,554 US Pat. No. 5,568,737 US Pat. No. 5,771,712 US Pat. No. 5,799,507 US Pat. No. 5,881,569 US Pat. No. 5,890,378 US Pat. No. 5,983,664 US Pat. No. 6,182,469 US Pat. No. 6,578,379 US Pat. No. 6,712,880 US Pat. No. 6,915,662 US Patent No. 7,191,617 US Pat. No. 7,219,513 US Reissue Patent No. 33,408 US patent application Ser. No. 11 / 430,412 US patent application Ser. No. 11 / 839,693 US patent application Ser. No. 11 / 971,491 US patent application Ser. No. 12 / 206,230 U.S. Patent Application No. 12 / 689,616 US patent application Ser. No. 12 / 717,394 US patent application Ser. No. 12 / 750,862 US patent application Ser. No. 12 / 772,472 U.S. Patent Application No. 12 / 781,259 US patent application Ser. No. 12 / 868,993 US patent application Ser. No. 12 / 869,007 US patent application Ser. No. 12 / 869,139 US patent application Ser. No. 12 / 979,563 US Patent Application No. 13 / 048,315

The present invention uses a novel means of performing the various steps described above more effectively and using less equipment. This is achieved by combining what has conventionally been individual equipment items into a common housing, thereby reducing the space required for the processing plant and reducing the capital cost of the equipment. Surprisingly, applicants have found that the smaller the equipment size, the lower the power consumption required to achieve a given recovery level, thereby increasing the processing efficiency and operating costs of the equipment. I found it smaller. In addition, the smaller the equipment size, the more piping that interconnects the individual equipment items in the traditional plant design can be omitted, thereby further reducing capital costs and the associated flange piping connections. It will be omitted. Piping flanges are potential sources of leakage of hydrocarbons (hydrocarbons are volatile organic compounds (VOCs) that can produce greenhouse gases and can be a precursor to atmospheric ozone production), so these flanges Omitting reduces the possibility of atmospheric radiation that can cause environmental destruction.

In accordance with the present invention, it has been found that C ₃ recovery can exceed 99.6% while the C ₂ component is substantially completely removed in the residual gas stream. In addition, the present invention is, while retaining the same recovery levels, the prior art compared to the substantially 100% separation of C ₂ components and lighter components from the C ₃ components and heavier components at lower energy requirements Make it possible to do. The present invention is applicable at lower pressures and higher temperatures, but feed gases above the range of 400-1500 psia (2,758-10,342 kPa (a)) can be used at -50 degrees Fahrenheit (-46 degrees Celsius). ) It is particularly advantageous when processing under conditions that require the following NGL recovery column top temperature.

  For a better understanding of the present invention, reference is made to the following examples and drawings.

4 is a flowchart of a prior art natural gas processing plant according to US Pat. No. 5,799,507. It is a flowchart of the natural gas processing plant which concerns on this invention. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream. 6 is a flowchart showing an alternative means of applying the present invention to a natural gas stream.

  In the following description of the above figure, a table summarizing the flow rates calculated for representative processing conditions is provided. In the table shown below, the value of the flow rate (unit: mol / hour) is rounded off for convenience. The total stream flow rates shown in the table all include non-hydrocarbon components and are therefore generally larger than the sum of the hydrocarbon component stream flow rates. The indicated temperature is an approximate value rounded off. It should be noted that the process design calculations performed to compare the processes shown in the drawings are based on the assumption that there is no heat leakage from ambient to process or from process to ambient. In view of the quality of commercially available insulation, this assumption is reasonable and it is common for those skilled in the art to make this assumption.

  For convenience, processing parameters are shown in both the traditional British unit system and the international unit system (SI). The molar flow rates shown in the table may be interpreted as pound moles per hour or kilogram moles per hour. The energy consumption expressed in horsepower (HP) and / or 1000 British heat / hour (MBTU / Hr) corresponds to a molar flow rate in pounds mol / hour. The energy consumption expressed in kilowatts (kW) corresponds to the molar flow rate expressed in kilogram moles / hour.

DESCRIPTION OF THE PRIOR ART FIG. 1 is a process flow diagram illustrating the design of a processing plant for recovering C ₃ + components from natural gas using the prior art according to US Pat. No. 5,799,507. In this process simulation, the incoming gas enters the plant as stream 31 at 110 degrees Fahrenheit (43 degrees Celsius) and 885 psia (6,100 kPa (a)). If the incoming gas contains a concentration of sulfur compounds that makes it impossible for the product stream to meet certain standards, the sulfur compounds should be subjected to appropriate pretreatment (not shown) of the feed gas. Is removed. In addition, the feed stream is generally dehydrated to prevent the formation of hydrates (ice) under cryogenic conditions. Solid desiccants are generally used for this purpose.

  Feed stream 31 is heated by heat exchange with cold residual gas (stream 44), instantaneously expanded separator liquid (stream 35a), and distillate at -105 degrees Fahrenheit (-76 degrees Celsius) (stream 43). It is cooled in the exchanger 31. The cooled stream 31a entered the separator 11 at -34 degrees Fahrenheit (-36 degrees Celsius) and 875 psia (6,031 kPa (a)), where the vapor (stream 34) was condensed. Separated from the liquid (stream 35). Separator liquid (stream 35) is expanded by expansion valve 12 to a pressure slightly higher than the operating pressure of fractionator 15 (about 375 psia (2,583 kPa (a))), so that stream 35a is Cool to -65 degrees Fahrenheit (-54 degrees Celsius). As stream 35a enters heat exchanger 10, the feed gas is cooled as described above, and stream 35b is 105 degrees Fahrenheit (41 degrees Celsius) before being fed to fractionator 15 at the lower center column feed point. To be heated.

  Steam (stream 34) emanating from the separator 11 flows into the operational expander 13 where mechanical energy is extracted from this portion of the high pressure feed. The operational expander 13 expands steam substantially isentropically to the operating pressure of the fractionation column 15 by an expansion operation that cools the expanded stream 34a to about −100 degrees Fahrenheit (−74 degrees Celsius). . A typical commercially available expander can recover as much as 80% to 85% of the work theoretically available in an ideal isentropic expansion. The recovered work is often used, for example, to drive a centrifugal compressor (such as item 14) that can be used to recompress the heated residual gas (stream 44a). The partially condensed expanded stream 34a is then fed as a feed to fractionator 15 at the upper central column feed point.

The deethanizer in fractionator 15 is a conventional distillation column comprising a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and 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.

  A portion of the distilled steam (stream 38) is drawn from the upper region of the removal zone 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 creates a driving force that allows the distillate vapor stream 38 to pass through the heat exchanger 17 and flow to the reflux separator 18. 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, resulting in 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 distilled in 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.

  The distillate stream 43 emanating from the deethanizer 15 is drawn from the lower region of the absorption zone 15 a and led to the heat exchanger 10. In the heat exchanger 10, the distillate stream 43 is heated as the incoming feed gas is cooled as described above. This liquid flow emanating from the deethanizer is generally due to thermosyphon circulation, but a pump may be used. This liquid stream is heated to −4 degrees Fahrenheit (−20 degrees Celsius) so that the stream 43a is partially evaporated before returning to the deethanizer 15 as a central column feed in the central region of the removal zone 15b. The

In the removal area 15b of deethanizer 15, the feed stream, methane and C ₂ components are removed. The resulting liquid product stream 37 escapes from the bottom of the tower at 201 degrees Fahrenheit (94 degrees Celsius). In this bottom product, the ratio of ethane to propane is 0.048: 1 based on moles. The low-temperature residual gas (stream 44) flows in the heat exchanger 10 so as to oppose the inflowing feed gas. In the heat exchanger 10, the stream 44 is heated to 98 degrees Fahrenheit (37 degrees Celsius) (stream 44a). The residual gas is then recompressed in two stages. The first stage is the compressor 14 driven by the expansion machine 13. The second stage is the compressor 20 driven by an auxiliary power source. The compressor 20 compresses the residual gas (stream 44c) to the sales flow path pressure. After cooling to 120 degrees Fahrenheit (49 degrees Celsius) in the discharge cooler 21, the residual gas stream 44d 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.

A summary of stream flow rates and energy consumption in the process shown in FIG. 1 is illustrated in the following table, namely Table 1.

DESCRIPTION OF THE INVENTION FIG. 2 shows a flowchart of processing according to the invention. The feed gas components and conditions considered in the process shown in FIG. 2 are the same as those in FIG. Therefore, by comparing the process of FIG. 2 with that of FIG. 1, the advantages of the present invention can be shown.

  In the process simulation of FIG. 2, the incoming gas flows into the plant as stream 31 and enters heat exchange means in the feed cooling zone 115 a in the process assembly 115. The heat exchange means may comprise a finned tube heat exchanger, a plate heat exchanger, an aluminum brazed heat exchanger, or other types of heat exchange devices including multi-path and / or multifunction heat exchangers. Good. The heat exchange means is between the stream 31 flowing through one path of the heat exchange means, the instantaneously expanded separator liquid (stream 35a), and the residual gas stream emanating from the condensation zone 115b in the processing assembly 115. It is configured to perform heat exchange. Stream 31 is cooled while heating the instantaneously expanded separator liquid and the residual gas stream. The first part of stream 31 (stream 32) is drawn from the heat exchange means after stream 31 is partially cooled to 25 degrees Fahrenheit (-4 degrees Celsius), while the remaining second part ( Stream 33) is further cooled and leaves the heat exchange means at -20 degrees Fahrenheit (-29 degrees Celsius).

  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, a plate heat exchanger, an aluminum brazed heat exchanger, or other types of heat exchange devices including multi-path and / or multi-function heat exchangers It may consist of. The heat and mass transfer means comprises a vapor portion of stream 32 flowing upward through one path of the heat and 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 continuously performs the function of transferring the substance between the vapor phase and the liquid phase by continuously contacting the condensed liquid and the vapor. As a result, a part of the steam is rectified.

  The 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 steam portion of the stream 33 mixes with the steam leaving the heat and mass transfer means, resulting in the formation of a stream 34. This stream 34 exits separator zone 115e at -31 degrees Fahrenheit (-35 degrees Celsius). A 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).

  Vapor (stream 34) emanating from the separator section 115e flows into the operational expander 13 where mechanical energy is extracted from this portion of the high pressure feed. The operational expander 13 is expanded to an operating pressure of the absorption zone 115c (approximately 380 psia (2,618 kPa (a))) by an expansion operation that cools the expanded stream 34a to approximately -98 degrees Fahrenheit (-72 degrees Celsius). The vapor is expanded substantially isentropically. The partially condensed expanded stream 34a is then fed as a feed to a region below the absorption zone 115c in the processing assembly 115.

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 -102 degrees Fahrenheit (-74 degrees Celsius)
Then, it is pulled out from the lower region of the absorption area 115c. 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, although 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 allows the first distillate vapor stream (stream 38) to be drawn from the upper region of the deethanization zone 115d and directed to the heat exchange means in the condensation zone 115b in the processing assembly 115. Will occur. 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. The heat exchange means is configured to exchange heat between a first distillate vapor stream 38 flowing through one path of the heat exchange means and a second distillate vapor stream rising from the absorption zone 115c in the processing assembly 115. It is a thing. The second distillate vapor stream is then heated while the stream 38 is allowed to cool and at least partially condense. Thereafter, the second distillate vapor stream flows out of the heat exchange means and is separated into respective 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. Due to this absorption cooling effect, the second distilled steam stream partially condenses the first distilled steam stream (stream 38) without operating the deethanizer section 115d at a pressure significantly higher than the pressure in the absorption section 115c. 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 distilled in 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, the distilled steam stream 38 will contain a minimum amount of these components.

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. The deethanized zone 115d also includes a heat / material transfer means below the material transfer means. This heat and mass transfer means is also a finned tube heat exchanger, a plate heat exchanger, an aluminum brazed heat exchanger, or other types of heat exchange devices including multi-path and / or multi-function heat exchangers It may consist of. The heat / mass transfer means includes a heating medium flowing through one path of the heat / mass transfer means, and a deethanizing section 115d.
The distillate stream is heated by exchanging heat with the distillate stream flowing downward from the substance transfer means. 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. The heat / mass transfer means also performs the function of transferring the mass between the vapor phase and the liquid phase by continuously contacting the removed steam and the distillate stream. 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 warmed second distilled steam stream mixes with all the steam separated from the cooled first distilled steam stream 38 as described above. 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.

  A summary of stream flow rates and energy consumption in the process shown in FIG. 2 is illustrated in the following table, Table 2.

  Comparison of Tables 1 and 2 shows that the present invention maintains substantially the same recovery as the prior art. However, a further comparison of Table 1 and Table 2 showed that the same product yield was achieved using less power than the prior art. From the perspective of recovery efficiency (defined by the amount of propane recovered per unit power), the present invention represents an improvement of over 5% over the prior art process of FIG.

  Compared to the prior art relating to the process of FIG. 1, the improvement in recovery efficiency provided by the present invention is mainly due to three factors. First, the compact configuration of the heat exchange means in the feed cooling zone 115a and the condensation zone 115b in the processing assembly 115 eliminates the pressure drop due to interconnect piping found in conventional processing plants. As a result, the residual gas flowing to the compressor 14 is higher in pressure for the present invention compared to the prior art. Thus, the residual gas flowing into the compressor 20 is at a significantly higher pressure, thereby lowering the power required by the present invention to restore the residual gas to line pressure.

  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 separated 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.

  In addition to improving processing efficiency, the present invention provides two other advantages over the prior art. First, the compact construction of the processing assembly 115 according to the present invention provides six equipment items in the prior art (heat exchangers 10 and 17, shown in FIG. 1, separator 11, reflux separator 18, reflux). The pump 19 and fractionator 15) are replaced by a single equipment item (processing assembly 115 shown in FIG. 2). This replacement reduces image space requirements, eliminates interconnect piping, and saves power consumed by the recirculation pump. As a result, the use of the present invention reduces the processing plant equipment and operating costs over the prior art. Secondly, the elimination of interconnect piping means that, compared to the prior art, the number of flange connections used in the processing plant utilizing the present invention is much smaller. As a result, the number of potential leak sources in the plant is reduced. Hydrocarbons are volatile organic compounds (VOCs), and some hydrocarbons are classified as greenhouse gases, and some can be precursors of atmospheric ozone formation. This means that the present invention reduces the possibility of atmospheric radiation that can lead to environmental destruction.

Other Embodiments In some circumstances, the feed cooling zone 115a and the condensation zone 115b are omitted from the processing assembly 115 and are external to the processing assembly, such as the heat exchanger 23 and the heat exchanger 17 shown in FIGS. It may be preferred to use one or more located heat exchange means for feed cooling and reflux condensation. Such a configuration allows the processing assembly 115 to be smaller, thereby reducing the overall plant cost and / or in some cases shortening the manufacturing schedule. It should be noted that in all cases, heat exchanger 23 and heat exchanger 17 may represent either a plurality of individual heat exchangers, a single multi-path heat exchanger, or any combination thereof. . Each such heat exchanging means may be a finned tube heat exchanger, a plate heat exchanger, an aluminum brazed heat exchanger, or other types of heat exchanging devices including multi-path and / or multi-function heat exchangers It may consist of. In some cases, it may be advantageous to consolidate feed cooling and reflux condensation into a single multifunction heat exchanger. When the heat exchanger 17 is located outside the processing assembly, the reflux separator 18 and pump 19 separate the condensed liquid stream 40 and deliver at least a portion of the stream 40 as reflux to the absorption zone 115c. Will generally be needed.

As described above with respect to the embodiment of the invention shown in FIG. 2, the first distillate steam stream 38 is partially condensed and the resulting condensed water is precious C ₃ from the steam exiting the operational expander. Used to absorb components 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. Depending on the composition of the feed gas stream, either in the condensation zone 115b (FIGS. 2-13) or in the heat exchanger 17 (FIGS. 14-21), an external It should be noted that it may be advantageous to use 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, the 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 12) or in heat exchanger 17 (FIGS. 16 and 20) is shown using distillate stream 43 to partially cool first distillate vapor stream 38. 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.)

Depending on the quality of the heavier hydrocarbons in the feed gas and the feed gas pressure, the cooled first part flows into the separator section 115e in FIGS. 2 and 14 or into the separator 11 in FIGS. 32 and the second portion 33 (or cooled into the separator section 115e in FIGS. 3-7 and 15-17, or into the separator 11 in FIGS. 9-13 and 19-21). The feed stream 31a) may not contain any liquid at all (because the temperature is higher than the dew point or the pressure is higher than the cricon denbar). In such a case, there is no liquid in the stream 35 (as indicated by the dotted line). In such circumstances, the separator section 115e (FIGS. 2-7 and 14-17) or the separator 11 (FIGS. 8-13 and 18-21) of the processing assembly 115 may not be necessary. is there.

  In accordance with the present invention, in particular in the case of a highly rich inflow gas, there is a cooling available for the inflow gas and / or for the first distillate vapor stream emanating from the second distillate 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 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, a plate heat exchanger, an aluminum brazed heat exchanger, or other types of heat exchange devices including multi-path and / or multi-function 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 and 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 FIGS. 2, 8, 14, and 18 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. If additional cooling of the first distillate steam stream is desired, the heat exchanger 10 (FIGS. 6 and 6) in the condensation zone 115b (FIGS. 2-5, 7-11, and 13) of the processing assembly 115 is shown. The heat exchange means in 12) or in the heat exchanger 17 (FIGS. 14-21) may comprise provisions for providing supplemental cooling using a 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 multi-path and / or multi-function heat exchange device is used to achieve the desired cooling and heating, stream 31, stream 32, stream 33, first distillate steam stream 38, cooled stream. Appropriate means for distributing, separating, and collecting all of the vapor separated from 38 and the second distillate vapor stream will be provided.

2-6, 8-12, 14-16, and 18-20, the relative amount of condensed liquid divided between stream 41 and stream 42 is the gas pressure, It should be recognized that it depends on several factors including the feed gas composition and the amount of horsepower available. Optimal partitioning is generally impossible to anticipate unless a particular situation is evaluated for a particular application of the present invention. In some circumstances, in stream 41, all of the condensed liquid is fed to the upper region of absorption zone 115c, and in stream 42, the upper region of deethanization zone 115d is shown as a dotted line with respect to stream 42. It may be preferable not to feed at all. In such a case, the heated distillate stream 43a may be fed to the upper region of the deethanization section 115d to function as a reflux.

The present invention provides a recovery of C ₃ components and heavier hydrocarbon components is improved with respect to the unit consumption of usufruct resources required carrying out the process. Improvements in consumption of utility resources required to perform processing are required to reduce power requirements for compression or recompression, reduce power requirements for external cooling, and reboiling towers It can appear in the form of reduced energy requirements or a combination of these.

  While examples have been described that are considered to be preferred embodiments of the invention, those skilled in the art will recognize that other and further modifications may be made without departing from the spirit of the invention as defined in the following claims. It will be appreciated that the present invention can be applied to various situations, different types of feeds, or other requirements.

Claims (45)

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) 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) a first distillate stream is collected from a lower region of the absorption means and supplied as an upper feed to a substance transfer means housed in the processing assembly;
(5) The first distilled steam stream is collected from the upper region of the substance transfer means, and is sufficiently cooled in the second heat exchange means, so that at least a part of the first distilled steam stream is condensed,
(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 distillate vapor stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least one part of the cooling of step (5);
(9) The heated second distilled steam stream is mixed with all of the residual steam stream, resulting in a mixed steam 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 substance transfer means and heated in the heat / substance transfer means accommodated in the processing assembly, whereby the more volatile components are removed from the second 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. An effective way to do. 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) 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 distilled steam stream is collected from the upper region of the substance transfer means, and is sufficiently cooled in the second heat exchange means, so that at least a part of the first distilled steam stream is condensed,
(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 distillate vapor stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least one part of the cooling of step (7);
(11) The heated second distilled steam stream is mixed with all of the residual steam stream, resulting in a mixed steam 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 substance transfer means and heated in the heat / substance transfer means accommodated in the processing assembly, whereby the higher volatility component is removed from the second 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. 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) 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 transmission means as an upper 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 partly condensed first distillation vapor stream is fed to a separation means and separated in the separation means, whereby the condensed stream and the first
A residual vapor stream is formed containing all of the uncondensed vapor remaining after the distillation vapor stream has been cooled;
(7) At least a portion of the condensed stream is fed as an upper feed to the absorption means;
(8) A second distillate steam 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 distilled steam stream is mixed with all of the residual steam stream, resulting in a mixed steam 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 substance transfer means and heated in the heat / substance transfer means accommodated in the processing assembly, whereby the more volatile components are removed from the second 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. 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) 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 transmission means as an upper 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 distillate vapor stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least one part of the cooling of step (7);
(11) The heated second distilled steam stream is mixed with all of the residual steam stream, resulting in a mixed steam 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 substance transfer means and heated in the heat / substance transfer means accommodated in the processing assembly, whereby the higher volatility component is removed from the second 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. 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) 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 accommodated 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 to the mass transfer means contained in the processing assembly,
(9) The first distilled steam stream is collected from the upper region of the mass transfer means, and is sufficiently cooled in the second heat exchange means, so that at least a part of the first distilled steam stream is condensed,
(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 distilled steam stream is collected from the upper region of the absorption means and heated in the second heat exchange means, thereby supplying at least one part of the cooling of step (9);
(13) The heated second distilled steam stream is mixed with all of the residual steam stream, resulting in the formation of a mixed steam 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 substance transfer means and heated in the second heat / substance transfer means accommodated in the processing assembly, whereby the more volatile components are removed. 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. 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) 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 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 part of the cooling of step (3), The heated first distillate stream is then fed as an upper feed to the mass transfer means contained in the processing assembly,
(10) The first distilled steam stream is collected from an upper region of the mass transfer means, and is sufficiently cooled in the second heat exchange means, so that at least a part of the first distilled steam stream is condensed,
(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) The second distillate steam stream is collected from the upper region of the absorption means and the second
Heated in the heat exchange means, thereby supplying at least one part of said cooling of step (10);
(14) The heated second distilled steam stream is mixed with all of the residual steam stream, resulting in a mixed steam 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 substance transfer means and heated in the second heat / substance transfer means accommodated in the processing assembly, whereby the more volatile components are 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. 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) 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 to the mass transfer means contained in the processing assembly;
(9) The first distilled 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 distilled steam stream is condensed,
(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 distilled steam stream is collected from the upper region of the absorption means and heated in the third heat exchange means, thereby supplying at least one part of the cooling of step (9);
(13) The heated second distilled steam stream is mixed with all of the residual steam stream, resulting in the formation of a mixed steam 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 substance transfer means and heated in the heat / substance transfer means accommodated in the processing assembly, whereby the more volatile component is removed from the first transfer means 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. 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) 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 to the mass transfer means contained in the processing assembly;
(11) The first distilled 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 distilled 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 distillate vapor stream is collected from the upper region of the absorption means and heated in the third heat exchange means, thereby supplying at least one part of the cooling of step (11);
(15) The heated second distillate 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 substance transfer means and heated in the heat / substance transfer means accommodated in the processing assembly, whereby the more volatile components are removed from the first transfer means. 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.   The method of claim 2, wherein the first separation means is housed in the processing assembly.   9. A method according to claim 4 or claim 8, wherein the first separating means is housed in the processing assembly.   7. A method according to claim 5 or claim 6, wherein the first separating means is housed in the processing assembly. (1) The heated first distillate stream is supplied to the substance transfer means at an intermediate feed position;
(2) the condensed stream is divided into at least a first reflux stream and a second reflux stream;
(3) the first reflux stream is supplied to the absorption means as the upper feed;
(4) The second reflux stream is supplied to the mass transfer means as the upper feed,
The method according to claim 3 or claim 7. (1) The heated first distillate stream is supplied to the substance transfer means at an intermediate feed position;
(2) the condensed stream is divided into at least a first reflux stream and a second reflux stream;
(3) the first reflux stream is supplied to the absorption means as the upper feed;
(4) The second reflux stream is supplied to the mass transfer means as the upper feed,
9. A method according to claim 4 or claim 8. (1) The heated first distillate stream is supplied to the substance transfer means at an intermediate feed position;
(2) the condensed stream is divided into at least a first reflux stream and a second reflux stream;
(3) the first reflux stream is supplied to the absorption means as the upper feed;
(4) The second reflux stream is supplied to the mass transfer means as the upper feed,
7. A method according to claim 5 or claim 6. (1) The heated first distillate stream is supplied to the substance transfer means at an intermediate feed position;
(2) the condensed stream is divided into at least a first reflux stream and a second reflux stream;
(3) the first reflux stream is supplied to the absorption means as the upper feed;
(4) The second reflux stream is supplied to the mass transfer means as the upper feed,
The method of claim 10. (1) The heated first distillate stream is supplied to the substance transfer means at an intermediate feed position;
(2) the condensed stream is divided into at least a first reflux stream and a second reflux stream;
(3) the first reflux stream is supplied to the absorption means as the upper feed;
(4) The second reflux stream is supplied to the mass transfer means as the upper feed,
The method of claim 11. (1) The gas collecting means is accommodated in the processing assembly,
(2) An additional heat / mass transfer means is provided in the gas collection means, and the additional heat / mass transfer means comprises one or more paths for an external refrigerant,
(3) The cooled gas stream is supplied to the gas collecting means and led to the additional heat and mass transfer means, and as a result, further cooled by the external refrigerant,
(4) the further cooled gas stream is expanded to the lower pressure and then fed to the absorption means as the bottom feed;
The method according to claim 1, claim 3, or claim 7. (1) The gas collecting means is accommodated in the processing assembly,
(2) An additional heat / mass transfer means is provided in the gas collection means, and the additional heat / mass transfer means comprises one or more paths for an external refrigerant,
(3) The cooled gas stream is supplied to the gas collecting means and led to the additional heat and mass transfer means, and as a result, further cooled by the external refrigerant,
(4) the further cooled gas stream is expanded to the lower pressure and then fed to the absorption means as the bottom feed;
The method of claim 12. (1) An additional heat / mass transfer means is provided in the first separation means, and the additional heat / mass transfer means includes one or a plurality of paths for an external refrigerant,
(2) The vapor stream is directed to the additional heat / mass transfer means and cooled by the external refrigerant, resulting in the formation of additional condensed water,
(3) The condensed water becomes a part of the at least one liquid stream separated in the first separation means.
The method of claim 2, claim 4, claim 8, or claim 9. (1) An additional heat / mass transfer means is provided in the first separation means, and the additional heat / mass transfer means includes one or a plurality of paths for an external refrigerant,
(2) The vapor stream is directed to the additional heat / mass transfer means and cooled by the external refrigerant, resulting in the formation of additional condensed water,
(3) The condensed water becomes a part of the at least one liquid stream separated in the first separation means.
The method of claim 10. (1) An additional heat / mass transfer means is provided in the first separation means, and the additional heat / mass transfer means includes one or a plurality of paths for an external refrigerant,
(2) The vapor stream is directed to the additional heat / mass transfer means and cooled by the external refrigerant, resulting in the formation of additional condensed water,
(3) The condensed water becomes a part of the at least one liquid stream separated in the first separation means.
The method of claim 13. (1) An additional heat / mass transfer means is provided in the first separation means, and the additional heat / mass transfer means includes one or a plurality of paths for an external refrigerant,
(2) The vapor stream is directed to the additional heat / mass transfer means and cooled by the external refrigerant, resulting in the formation of additional condensed water,
(3) The condensed water becomes a part of the at least one liquid stream separated in the first separation means.
The method of claim 15. 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 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) 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) first vapor collection means received in the processing assembly and connected to the substance transfer means for receiving a first distillation vapor stream from an upper region of the substance 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 exchange further connected to the second steam collection means for supplying at least a portion of the cooling of step (7) by receiving and heating the second distillation steam stream 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) second liquid collection means contained in the processing assembly and connected to the substance transfer means for receiving a second distillate stream from a lower region of the substance 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 housed in the processing assembly and connected to the second liquid collecting means for discharging from the processing assembly as the relatively low volatility fraction;
(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;
A device comprising: 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 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) first vapor collection means contained in the processing assembly and connected to the substance transfer means for receiving a first distillation vapor stream from an upper region of the substance 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 collecting means contained in the processing assembly and connected to the substance transfer means for receiving a second distillate stream from a lower region of the substance 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 housed 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: 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 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 means contained in the processing assembly and connected to the second heat exchange means for receiving the heated first distillate stream as an upper feed to the mass transfer means;
(7) first vapor collection means contained in the processing assembly and connected to the substance transfer means for receiving a first distillation vapor stream from an upper region of the substance 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; 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) a second liquid collecting means contained in the processing assembly and connected to the substance transfer means for receiving a second distillate stream from a lower region of the substance 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 housed 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: 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 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 means contained in the processing assembly and connected to the second heat exchange means for receiving the heated first distillate stream as an upper feed to the mass transfer means;
(9) a first vapor collection means contained in the processing assembly and connected to the substance transfer means for receiving a first distillation vapor stream from an upper region of the substance 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; 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 substance transfer means for receiving a second distillate stream from a lower region of the substance 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 housed 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: 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 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 A 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); Substance transfer means;
(10) The substance transfer means contained in the processing assembly and connected to the first heat and substance transfer means for receiving the heated first distillate stream as an upper feed to the substance transfer means. When,
(11) a first vapor collection means contained in the processing assembly and connected to the substance transfer means for receiving a first distillation vapor stream from an upper region of the substance 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 substance transfer means for receiving a second distillate stream from a lower region of the substance 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; 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: 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 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 contained in the first separation means and the dividing means A first heat and mass transfer means connected to the
(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); Substance transfer means;
(11) The substance transfer means contained in the processing assembly and connected to the first heat / substance transfer means for receiving the heated first distillate stream as an upper feed to the substance transfer means When,
(12) first steam collection means received in the processing assembly and connected to the substance transfer means for receiving a first distillation vapor stream from an upper region of the substance 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 substance transfer means for receiving a second distillate stream from a lower region of the substance 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; 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: 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 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); Substance transfer means;
(10) the mass transfer means contained in the processing assembly and connected to the second heat exchange means for receiving the heated first distillate stream as an upper feed to the mass transfer means;
(11) a first vapor collection means contained in the processing assembly and connected to the substance transfer means for receiving a first distillation vapor stream from an upper region of the substance 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 substance transfer means for receiving a second distillate stream from a lower region of the substance 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 housed 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: 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 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); Substance transfer means;
(12) the mass transfer means contained in the processing assembly and connected to the second heat exchange means for receiving the heated first distillate stream as an upper feed to the mass transfer means;
(13) first vapor collection means contained in the processing assembly and connected to the substance transfer means for receiving a first distillation vapor stream from an upper region of the substance transfer means;
(14) receiving said first distillation steam stream, connected to said first steam collecting means for sufficiently cooling said first distillation steam stream and condensing at least a part of said first distillation 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 substance transfer means for receiving a second distillate stream from a lower region of the substance 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 housed 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:   25. The apparatus of claim 24, wherein the first separation means is housed in the processing assembly.   27. The apparatus of claim 26, wherein the first separation means is housed in the processing assembly.   29. An apparatus according to claim 27 or claim 28, wherein the first separating means is housed in the processing assembly.   32. The apparatus of claim 30, wherein the first separation means is housed in the processing assembly. (1) the mass transfer means is configured to be connected to the second heat exchange means for receiving the heated first distillate stream at an intermediate feed position;
(2) The dividing means is configured to receive the condensed stream and be connected to the separating means to divide the condensed stream into at least a first circulating stream and a second circulating stream. ,
(3) the absorbing means is configured to be connected to the dividing means to receive the first reflux stream as the upper feed to the absorbing means;
(4) The mass transfer means is configured to be connected to the dividing means to receive the second reflux stream as the upper feed to the mass transfer means,
26. The device of claim 25. (1) the mass transfer means is configured to be connected to the second heat exchange means for receiving the heated first distillate stream at an intermediate feed position;
(2) The additional dividing means is connected to the separating means for receiving the condensed stream and dividing the condensed stream into at least a first reflux stream and a second reflux stream. Configured,
(3) the absorbing means is configured to be connected to the additional dividing means to receive the first reflux stream as the upper feed to the absorbing means;
(4) The mass transfer means is configured to be connected to the additional splitting means to receive the second reflux stream as the upper feed to the mass transfer means,
30. Apparatus according to claim 29. (1) the mass transfer means is configured to be connected to the second heat exchange means for receiving the heated first distillate stream at an intermediate feed position;
(2) the dividing means is connected to the second separating means for receiving the condensed stream and dividing the condensed stream into at least a first circulating stream and a second circulating stream;
(3) the absorbing means is configured to be connected to the dividing means to receive the first reflux stream as the upper feed to the absorbing means;
(4) The mass transfer means is configured to be connected to the dividing means to receive the second reflux stream as the upper feed to the mass transfer means,
27. Apparatus according to claim 26. (1) The mass transfer means is configured to be connected to the first heat / mass transfer means to receive the heated first distillate stream at an intermediate feed position,
(2) An additional dividing means is connected to the second separating means for receiving the condensed stream and dividing the condensed stream into at least a first reflux stream and a second reflux stream. ,
(3) the absorbing means is configured to be connected to the additional dividing means to receive the first reflux stream as the upper feed to the absorbing means;
(4) The mass transfer means is configured to be connected to the additional splitting means to receive the second reflux stream as the upper feed to the mass transfer means,
29. Apparatus according to claim 27 or claim 28. (1) the mass transfer means is configured to be connected to the second heat exchange means for receiving the heated first distillate stream at an intermediate feed position;
(2) An additional dividing means is connected to the second separating means for receiving the condensed stream and dividing the condensed stream into at least a first reflux stream and a second reflux stream. ,
(3) the absorbing means is configured to be connected to the additional dividing means to receive the first reflux stream as the upper feed to the absorbing means;
(4) The mass transfer means is configured to be connected to the additional splitting means to receive the second reflux stream as the upper feed to the mass transfer means,
35. Apparatus according to claim 30 or claim 34. (1) the mass transfer means is configured to be connected to the second heat exchange means for receiving the heated first distillate stream at an intermediate feed position;
(2) the dividing means is connected to the second separating means for receiving the condensed stream and dividing the condensed stream into at least a first circulating stream and a second circulating stream;
(3) the absorbing means is configured to be connected to the dividing means to receive the first reflux stream as the upper feed to the absorbing means;
(4) The mass transfer means is configured to be connected to the dividing means to receive the second reflux stream as the upper feed to the mass transfer means,
33. The apparatus according to claim 32. (1) The mass transfer means is configured to be connected to the first heat / mass transfer means to receive the heated first distillate stream at an intermediate feed position,
(2) An additional dividing means is connected to the second separating means for receiving the condensed stream and dividing the condensed stream into at least a first reflux stream and a second reflux stream. ,
(3) the absorbing means is configured to be connected to the additional dividing means to receive the first reflux stream as the upper feed to the absorbing means;
(4) The mass transfer means is configured to be connected to the additional splitting means to receive the second reflux stream as the upper feed to the mass transfer means,
34. Apparatus according to claim 33. (1) The gas collecting means is accommodated in the processing assembly,
(2) An additional heat / mass transfer means is provided in the gas collection means, and the additional heat / mass transfer means comprises one or more paths for an external refrigerant,
(3) The gas collecting means receives the cooled gas stream and guides the cooled gas stream to the additional heat / mass transfer means, whereby the cooled gas stream is transferred to the external refrigerant. Connected to the first heat exchange means for further cooling by
(4) The expansion means receives the further cooled gas stream, expands the further cooled gas stream to the lower pressure, and the expansion means is further connected to the absorption means. Configured to be connected to the gas collecting means for supplying the expanded, further cooled gas stream as the bottom feed to the expansion means,
36. An apparatus according to claim 23, claim 25, or claim 35. (1) The gas collecting means is accommodated in the processing assembly,
(2) An additional heat / mass transfer means is provided in the gas collection means, and the additional heat / mass transfer means comprises one or more paths for an external refrigerant,
(3) The gas collecting means receives the cooled gas stream, guides the cooled gas stream to the additional heat / material transfer means, and further cools the cooled gas stream by the external refrigerant. Connected to the first mixing means,
(4) The expansion means receives the further cooled gas stream, expands the further cooled gas stream to the lower pressure, and the expansion means is further connected to the absorption means. Configured to be connected to the gas collecting means for supplying the expanded, further cooled gas stream as the bottom feed to the expansion means,
37. An apparatus according to claim 29 or claim 36. (1) An additional heat / mass transfer means is provided in the first separation means, and the additional heat / mass transfer means includes one or a plurality of paths for an external refrigerant,
(2) The vapor stream is directed to the additional heat / mass transfer means and cooled by the external refrigerant, resulting in the formation of additional condensed water,
(3) The condensed water becomes a part of the at least one liquid stream separated in the first separation means.
41. An apparatus according to claim 24, claim 26, claim 30, claim 31, claim 32, claim 34, claim 37, or claim 40. (1) An additional heat / mass transfer means is provided in the first separation means, and the additional heat / mass transfer means includes one or a plurality of paths for an external refrigerant,
(2) The vapor stream is directed to the additional heat / mass transfer means and cooled by the external refrigerant, resulting in the formation of additional condensed water,
(3) The condensed water becomes a part of the at least one liquid stream separated in the first separation means.
40. The apparatus of claim 39.

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