JP5798180B2 - Hydrocarbon gas treatment - Google Patents

Description

  Ethylene, ethane, propylene, propane, and / or heavier hydrocarbons can be obtained from other hydrocarbon materials such as coal, crude oil, naphtha, oil shale, tar sand, lignite, natural gas, refinery gas, And can be recovered from various gases such as synthesis gas flow. Natural gas usually has a major proportion of methane and ethane. That is, both methane and ethane contain at least 50 mole percent of the gas. The gas may also contain relatively small amounts of heavier hydrocarbons such as propane, butane, pentane as well as hydrogen, nitrogen, carbon dioxide and other gases.

The present invention generally relates to the recovery of ethylene, ethane, propylene, propane, and heavier hydrocarbons from such gas streams. Typical analysis of the gas stream to be treated according to the invention, in terms of mole percent on the estimate, of 90.0% methane, 4.0% ethane and other C ₂ components, 1.7% propane and other C ₃ component, 0.3% isobutane, 0.5% normal butane, plus 0.8% pentane, the balance being composed of nitrogen and carbon dioxide. Sulfur containing gases may also be present.

  Historically repeated price fluctuations in natural gas and its natural gas liquid (NGL) components can sometimes reduce incremental values of ethane, ethylene, propane, propylene, and heavier components as liquid products. there were. This has resulted in a need for processes that provide more efficient recovery of these products and processes that can provide efficient recovery with lower capital investment. Processes that can be used to separate these materials include processes based on gas cooling and freezing, oil adsorption, and frozen oil adsorption. In addition, cryogenic processing has become commonplace due to the availability of economical equipment that expands and extracts heat from the gas being processed while producing electrical power. Depending on the pressure of the gas source, the concentration of the gas (ethane, ethylene, and heavy hydrocarbon content), and the desired end product, each of these treatments, or a combination thereof, may be utilized.

  Currently, cryogenic expansion processes are generally preferred for natural gas liquid recovery because they provide maximum simplicity with ease of start-up, operational flexibility, high efficiency, safety and good reliability. U.S. Pat.Nos. 3,292,380, 4,061,481, 4,140,504, 4,157,904, 4,171,964, 4,185,978, No. 4,251,249, No. 4,278,457, No. 4,519,824, No. 4,617,039, No. 4,687,499, No. 4,689,063, No. 4 , 690,702, 4,854,955, 4,869,740, 4,889,545, 5,275,005, 5,555,748, 5,566 , 554, 5,568,737, 5,771,712, 5,799,507, 5,881,569, 5,890,378, 5,983,664 No. 6,182,469, No. 6,578,379, No. 6,71 880, No. 6,915,662, No. 7,191,617, No. 7,219,513, U.S. Pat. No. 33,408, and co-pending application No. 11 / 430,412. 11 / 839,693, 11 / 971,491, 12 / 206,230, 12 / 689,616, 12 / 717,394, 12 / 750,862, 12 / 772,472, 12 / 781,259, 12 / 868,993, 12 / 869,007, 12 / 869,139, and 12 / 979,563 (However, the description of the invention in some cases is based on processing conditions that are different from those described in the cited US patents).

In a typical cryogenic expansion recovery process, the pressurized feed gas stream is cooled by heat exchange with other streams of the process and / or an external refrigeration source, such as a propane compression-refrigeration system. As the gas is cooled, the liquid was concentrated, it is collected in one or more separators as high-pressure liquids containing some of the desired C _{2 +} components. Depending on the richness of the gas and the amount of liquid formed, the high pressure liquid can be expanded and fractionated to a lower pressure. Vaporization that occurs during liquid expansion causes further cooling of the flow. Under some conditions, it may be desirable to pre-cool the high pressure liquid prior to expansion to further reduce the temperature resulting from expansion. The expanded stream consisting of a mixture of liquid and vapor is fractionated in a distillation (demethanizer, deethanizer) column. In the column, the expansion cooled stream (s) is, as a lower liquid product, the desired C ₂ components, as the top portion steam from C ₃ components, and heavier hydrocarbon components, remaining Methane, nitrogen, and other volatile gases, or as the bottom liquid product, as the overhead vapor from the desired C ₃ component and heavier hydrocarbons, residual methane, C Distilled to separate the _two components, nitrogen and other volatile gases.

  If the feed gas is not fully concentrated (usually not concentrated), the vapor remaining from the partial concentration can be divided into two streams. One portion of the vapor is passed through a work expander or engine, an expansion valve, resulting in a lower pressure where additional liquid is concentrated as a result of further cooling of the flow. The pressure after expansion is essentially the same as the pressure at which the distillation column is operated. The combined gas-liquid phase resulting from the expansion is fed to the column as a feed.

  The remainder of the steam is cooled to a substantial concentrate by heat exchange with other process streams such as the top of the cold fractionation tower. Some or all of the high pressure liquid can be combined with this vapor prior to cooling. The resulting cooled stream is then expanded through a suitable expansion device such as an expansion valve to the pressure at which the demethanizer tower is operated. During expansion, some of the liquid evaporates, resulting in cooling of the entire stream. The flash expanded stream is then fed as an upper feed to the demethanizer tower. Usually, the vapor portion of the flash expanded stream and the top vapor of the demethanizer tower combine in the upper separator section of the fractionator as residual methane product gas. Alternatively, a cooled and expanded stream may be supplied to the separator to provide a vapor stream and a liquid stream. Vapor is combined with the top of the tower and liquid is fed to the column as an upper column feed.

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 No. 5,771,712 No. 5,799,507 No. 5,881,569 No. 5,890,378 No. 5,983,664 No. 6,182,469 No. 6,578,379 No. 6,712,880 No. 6,915,662 No. 7,191,617 No. 7,219,513 Reissued US 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

  The present invention utilizes a novel means for performing the various steps described above more efficiently and using a smaller number of devices. This is to integrate what was previously an individual equipment item into one common enclosure, thereby reducing the site space required for the processing plant and reducing the capital cost of the facility. Achieved by: Surprisingly, Applicants have found that a more compact arrangement significantly reduces the power consumption required to achieve a given recovery level, thereby increasing processing efficiency and reducing facility operating costs I also noticed to do. In addition, a more compact arrangement eliminates much of the piping used to interconnect individual equipment items in traditional factory designs, further reducing capital costs and eliminating associated flanged piping connections. To do. Piping flanges are a potential source of leakage for hydrocarbons (volatile organic compounds, VOCs that contribute to greenhouse gases and may be precursors of atmospheric ozone formation), thus eliminating these flanges That reduces the possibility of atmospheric emissions that may harm the environment.

In accordance with the present invention, it has been found that a CO ₂ recovery greater than 88% can be achieved. Similarly, in those instances where C ₂ component recovery is not desired, a C ₃ recovery greater than 93% can be maintained. In addition, the present invention differs from the prior art, while maintaining the same recovery levels, methane (or C ₂ components) and lighter components, C ₂ components at lower energy requirements (or C ₃ components ) And essentially 100% separation from heavier components. The present invention is applicable at lower pressures and warmer temperatures, but under conditions that require -50 ° F. [-46 ° C.] or lower NGL recovery column head temperature, 400 to 1500 psia [ 2,758 to 10,342 kPa (a)] or more is particularly advantageous when processing the feed gas.

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

FIG. 2 is a flow diagram of a prior art natural gas processing plant according to US Pat. No. 4,157,904. It is a flowchart of the natural gas processing factory by this invention. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream. FIG. 6 is a flow diagram showing an alternative means of application of the present invention to a natural gas stream.

  In the following description of the above figure, a table is provided that summarizes the flow rates calculated for representative process conditions. In the tables displayed herein, flow rate values (in moles per hour) are rounded to the nearest integer for convenience. Since the total flow shown in the table includes all non-hydrocarbon components, it is generally greater than the sum of the flow of hydrocarbon components. The temperatures shown are approximate values rounded to the nearest degree. The process design calculations performed to compare the processes shown in the figure are based on the assumption that there is no heat leakage from (or to) the environment to (or from) the process Please also note. The quality of commercially available insulation is a very reasonable assumption and usually made by those skilled in the art.

  For convenience, process parameters are reported in both traditional British units and System International d'Units (SI). The molar flow rates shown in the table can be interpreted as either pound moles / hour or kilogram moles / hour. Energy consumption, reported as horsepower (HP) and / or thousand British thermal units / hour (MBTU / Hr), corresponds to the indicated molar flow rate in lbmol / hour. The energy consumption reported as kilowatts (kW) corresponds to the indicated molar flow rate in kilogram moles / hour.

FIG. 1 is a process flow diagram illustrating the design of a processing plant for recovering C ₂ + components from natural gas using the prior art according to US Pat. No. 4,157,904. In this simulation of the process, the inlet gas enters the factory as stream 31 at 101 ° F. [39 ° C.] and 915 psia [6,307 kPa (a)]. If the inlet gas contains a sulfur component concentration that prevents the product stream from meeting specifications, the sulfur component is removed by appropriate pretreatment of a feed gas (not shown). In addition, the feed stream is usually dehydrated to prevent the formation of hydrates (ice) under cryogenic conditions. For this purpose, solid desiccants have usually been used.

  Feed stream 31 is divided into two parts, streams 32 and 33. Stream 32 is cooled to -31 ° F [-35 ° C] in heat exchanger 10 by heat exchange with the cold residual gas (stream 41a). On the other hand, stream 33 is heated by heat exchange with the demethanizer reboiler liquid (stream 43) at 43 ° F [6 ° C] and the side reboiler liquid (stream 42) at -47 ° F [-44 ° C]. Cool to −37 ° F. [−38 ° C.] in exchanger 11. Streams 32a and 33a recombine to form stream 31a. Stream 31a enters separator 12 where vapor (stream 34) is separated from concentrated liquid (stream 35) at -33 ° F [-36 ° C] and 893 psia [6,155 kPa (a)].

Vapor from separator 12 (stream 34) is divided into two streams, 36 and 39. Stream 36 containing about 32% of the total vapor is combined with separator liquid (stream 35), and combined stream 38 is combined with cold residue gas (stream 41) that is cooled to a substantial concentrate. The heat exchanger 13 passes through the heat exchanger. The resulting substantially concentrated stream -a at -131 ° F [-90 ° C] is then passed through expansion valve 14 to the operating pressure of fractionator 18 (approximately 410 psia [2,827 kPa (a) During expansion, a portion of the flow is vaporized, resulting in cooling of the entire flow, and in the process shown in Figure 1, the expanded flow 38b leaving the expansion valve 14 is -137 ° F [- 94 ° C.] and supplied to the separator portion 18a in the upper region of the fractionating column 18. The liquid separated there becomes an upper feed to the demethanizer 18b.

  The remaining 68% of the steam from the separator 12 (stream 39) enters the work expander 15 where mechanical energy is extracted from this portion of the high pressure feed. This machine 15 expands steam to column operating pressure substantially isentropically, and the work expansion cools the expanded stream 39a to a temperature of about -97 ° F [-72 ° C]. A typical commercially available expander can recover about 80-85% of the theoretically available work with ideal isentropic expansion. The recovered work is often used to drive a centrifugal compressor (such as 16) that can be used, for example, to recompress the residual gas (stream 41b). The partially concentrated expanded stream 39a is then fed to the fractionation tower 18 as a feed at the intermediate column feed point.

  The demethanizer tower in column 18 is a conventional distillation column that includes a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing materials. As is common in natural gas processing plants, the fractionation tower can be composed of two parts. The upper part 18a is a separator, and the partially vaporized upper feed is divided into respective vapor parts and liquid parts, and the vapor rising from the lower distillation part or demethanization part 18b is the vapor part of the upper feed. To form the top vapor (stream 41) of the low temperature demethanizer tower leaving the top of the tower at -136 ° F [-93 ° C]. The lower demethanizer 18b contains trays and / or fillers and provides the necessary contacts between the liquid falling downward and the vapor rising upward. Also, the demethanizer 18b heats and evaporates a portion of the liquid flowing down the column, stripping vapor flowing upward through the column to remove methane and the lighter component liquid product, stream 44. Also included are reboilers (such as the reboilers and side reboilers described above).

The liquid product stream 44 exits the bottom of the column at 65 ° F. [19 ° C.] based on a typical specification of a methane to ethane ratio of 0.010: 1 based on the mass in the bottom product. The residual gas (demethanizer top vapor stream 41) is in heat exchanger 13 where it is heated to -44 ° F [-42 ° C] (stream 41a) and it is 96 ° F [36 ° C. ] (Flow 41b) in the heat exchanger 10 heated to flow back to the incoming supply gas. The residual gas is then recompressed in two stages. The first stage is the compressor 16 driven by the expander 15. The second stage is the compressor 20 driven by a supplemental power source that compresses the residue gas (stream 41d) to the sales line pressure. After cooling to 120 ° F. [49 ° C.] in the exhaust cooler 21, the residual gas product (stream 41e) is 915 psia [6,307 kPa] sufficient to meet line requirements (usually at approximately inlet pressure). (A)] flows into the gas pipeline for sale.

A summary of flow and energy consumption for the process shown in FIG. 1 is set forth in the following table.

  FIG. 2 shows a flow diagram of the process according to the invention. The feed gas composition and conditions considered in the process presented in FIG. 2 are the same as in FIG. Accordingly, the process of FIG. 2 can be compared to the process of FIG. 1 to illustrate the advantages of the present invention.

In the simulation of the process of FIG. 2, the inlet gas enters the factory as stream 31 and is split into two parts, streams 32 and 33. The first portion, i.e. stream 32, enters the heat exchange means in the upper region of the feed cooler 118a within the processing assembly 118. This heat exchange means consists of fin and tube heat exchangers, plate heat exchangers, brazed aluminum heat exchangers, or other types of heat transfer devices including multi-pass and / or multi-service heat exchangers Can be done. This heat exchange means is a distillation resulting from a stream 32 flowing through one flow path of the heat exchange means and a separator portion 118b inside the processing assembly 118 heated by the heat exchange means in the lower region of the feed cooler 118a. It is configured to achieve heat exchange with the steam flow. Stream 32 is cooled while further heating the distillation vapor stream, and stream 32a leaves the heat exchange means at -26 ° F [-32 ° C].

The second part, stream 33, enters the heat and mass transfer means of the demethanizer 118d in the processing assembly 118. This heat and mass transfer means may also be other types of heat transfer , including fin and tube heat exchangers, plate heat exchangers, brazed aluminum heat exchangers, or multipass and / or multiservice heat exchangers It can consist of devices. The heat and mass transfer means may provide heat exchange between the flow 33 flowing through one flow path of the heat and mass transfer means and the distillate liquid flow flowing downward from the absorber 118c inside the processing assembly 118. Thus, stream 33 is cooled while it heats the distilled liquid stream and cools stream 33a to -38 ° [-39 ° C] before it leaves the heat and mass transfer means. When the distillation liquid stream is heated, a portion of it is vaporized, forming a stripping vapor that rises upward as the remaining liquid continues to flow downstream through the heat and mass transfer means. The heat and mass transfer means is capable of stripping steam and vapor so that it achieves mass transfer between the gas phase and the liquid phase and also functions to remove the liquid product stream 44 of methane and lighter components. Provide a continuous contact between the distilled liquid streams.

  Streams 32a and 33a recombine to form a stream 31a that enters separator portion 118e inside processing assembly 118 at −30 ° F. [−34 ° C.] and 898 psia [6,189 kPa (a)], resulting in steam ( Stream 34) is separated from the concentrated liquid (stream 35). Separator portion 118e has an internal head or other means to separate it from demethanizer 118d, so that the two portions within processing assembly 118 can operate at different pressures.

Vapor (stream 34) from separator portion 118e is split into two streams 36 and 39. Stream 36 containing about 32% of the total vapor is combined with the separated liquid (stream 35 via stream 37A), and combined stream 38 is in the lower region of feed cooler 118a within processing assembly 118. Enter the heat exchanger. This heat exchanger means may also be of other types, including fin and tube heat exchangers, plate heat exchangers, brazed aluminum heat exchangers, or multipass and / or multiservice heat exchangers. It can consist of a heat transfer device. The heat exchanger means is configured to achieve heat exchange between the stream 38 flowing through one flow path of the heat exchanger means and the distillation steam stream originating from the separator portion 118b, so that the stream 38 is distilled steam. The stream is cooled to a substantial concentrate while heating.

  The resulting substantially concentrated −130 ° F. [−90 ° C.] stream 38a then passes through the expansion valve 14 to the operating pressure of the absorber 118c (absorber) within the processing assembly 118 (approximately 415 psia [ 2,861 kPa (a)]). During expansion, a portion of the flow is vaporized, resulting in overall flow cooling. In the process shown in FIG. 2, the expanded stream 38 b leaving the expansion valve 14 reaches a temperature of −136 ° F. [−94 ° C.] and is supplied to the separator portion 118 b inside the processing assembly 118. The liquid separated therein is directed to the absorber 118c, while the remaining vapor combines with the vapor rising from the absorber 118c to form a distillate vapor stream that is heated in the cooler 118a.

The remaining 68% of the steam from separator portion 118e (stream 39) enters work expander 15 where mechanical energy is extracted from this portion of the high pressure feed. The machine 15 expands steam substantially isentropically to the operating pressure of the absorber 118c, and the work expansion cools the expanded stream 39a to about -94 ° F [-70 ° C]. The partially concentrated expanded stream 39a is then fed as a feed to the lower region of the absorber 118c within the processing assembly 118.

Absorber 118c includes a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and fillers. The tray and / or filler of the absorber 118c provides the necessary contact between the rising vapor and the cryogenic liquid falling downward. The liquid portion of the expanded stream 39a mixes with the liquid falling downward from the absorber 118c, and the combined liquid continues downward into the demethanizer 118d. The stripping vapor rising from the demethanizer 118d is combined with the vapor portion of the expanded flow 39a, comes up through the absorber 118c, comes into contact with the cryogenic liquid falling down, and has C ₂ component, C ₃ component, And heavier components are concentrated and absorbed from these vapors.

Distillation liquid flowing down from the heat and mass transfer means of the demethanizer 118d within the processing assembly 118 has been stripped of methane and lighter components. The resulting liquid product (stream 44) exits the lower region of the demethanizer 118d and leaves the processing assembly 118 at 67 ° F. [20 ° C.]. The distillate vapor stream resulting from separator portion 118b is warmed in feed cooler 118a as it provides cooling to streams 32 and 38, as described above, and the resulting residue gas stream 41 is 96 ° F [ 36 ° C.] to leave the processing assembly 118a. The residual gas is then recompressed in two stages: a compressor 16 driven by an expander 15 and a compressor 20 driven by a supplemental power source. After stream 41b is cooled to 120 ° F. [49 ° C.] in discharge cooler 21, the residual gas product (stream 41c) flows to the sales gas pipeline at 915 psia [6,307 kPa (a)].

A summary of the flow rate and energy consumption for the process shown in FIG. 2 is set forth in the following table.

  A comparison of Tables I and II shows that the present invention maintains essentially the same recovery as the prior art. However, a further comparison of Tables I and II shows that product yields were achieved with significantly less power than the prior art. In terms of recovery efficiency (defined by the amount of ethane recovered per unit of power), the present invention represents an approximately 7% improvement over the prior art of the process of FIG.

The improvement in recovery efficiency provided by the present invention over the recovery efficiency of the prior art of FIG. 1 is mainly due to two factors. First, the compact arrangement of heat exchange means in the feed cooling section 118a and heat exchange means in the heat and mass transfer means in the demethanizer section 118d is imposed by the interconnect piping found in conventional processing plants. Eliminate pressure drop. As a result, the portion of the feed gas flowing into the expander 15 is at a higher pressure relative to the present invention compared to the prior art, and the expander 15 of the present invention has a lower outlet pressure than the prior art expander 15. Makes it possible to generate as much power at higher outlet pressures as can be generated at Thus, the absorber 118c in the processing assembly 118 of the present invention can operate at a higher pressure than the prior art fractionation column 18 while maintaining the same recovery level. This higher operating pressure also adds a reduction in pressure drop to the residue gas due to the elimination of interconnect piping, resulting in a significantly higher pressure for the residue gas entering the compressor 20, thereby reducing the pipeline pressure according to the present invention. Reduce the power required to restore residual gas.

Second, the heat and mass transfer means of the demethanizer 118d to simultaneously heat the distilled liquid leaving the absorber 118c while allowing the resulting vapor to contact the liquid and remove its volatile components. Is more efficient than using a conventional distillation column with an external reboiler. Volatile components are continuously stripped of liquid, reducing the concentration of volatile components in the stripping vapor more quickly, thereby improving stripping efficiency for the present invention.

  In addition to increasing processing efficiency, the present invention provides two other advantages over the prior art. First, the compact arrangement of the processing assembly 118 of the present invention simply separates five prior art equipment items (heat exchangers 10, 11, and 13, separator 12, and fractionator 18 of FIG. 1). Replace with one equipment item (processing assembly 118 in FIG. 2). This reduces site space requirements, eliminates interconnect piping, and reduces the capital cost of the process plant utilizing the present invention that exceeds the capital cost of the prior art. Second, the elimination of mutual piping means that the processing plant utilizing the present invention has much fewer flanged connections than the prior art, reducing the number of potential leak sources in the plant. To do. Hydrocarbons are volatile organic compounds (VOCs), some of which are classified as greenhouse gases, some of which may be precursors of atmospheric ozone formation. This means that the present invention reduces the possibility of atmospheric emissions that can harm the environment.

(Other embodiments)
In some situations, it is preferred to eliminate the feed cooler 118a from the processing assembly 118 and use external heat exchange means for the feed cooling processing assembly, such as the heat exchanger 10 shown in FIGS. May be. Such an arrangement allows the processing assembly 118 to be smaller, in some cases reducing overall plant costs and / or shortening production schedules. Note that in all cases, exchanger 10 represents either a number of individual heat exchangers, or a single multi-pass heat exchanger, or a combination thereof. Each such heat exchanger may be a fin and tube heat exchanger, a plate heat exchanger, a brazed aluminum heat exchanger, or other types of heat transfer , including multi-pass and / or multi-service heat exchangers. It can consist of devices.

  In some situations, the liquid flow 35 is directed to the lower region of the absorber 118c via the flow 40 shown in FIGS. 2, 4, 6, 8, 10, 12, 14, and 16. It may be preferred to supply directly. In such a case, a suitable expansion device (such as expansion valve 17) is used to expand the liquid to the operating pressure of the absorption section 118c, and the resulting expansion liquid flow 40a is represented by the absorption section 118c (shown in broken lines). Is supplied as a feed to the lower region of In some situations, the liquid stream 35 (stream 37) is streamed with the vapor of stream 36 (FIGS. 2, 6, 10, and 14) or the cooled second portion 33a (FIGS. 4, 8, 12 and 16) to form a combined flow 38 and it may be preferred to send the remainder of the liquid flow 35 to the lower region of the absorber 118c via the flow 40 / 40a. is there. In some situations, the expanded liquid stream 40a is combined with the expanded stream 39a (FIGS. 2, 6, 10, and 14) or the expanded stream 34a (FIGS. 4, 8, 12, and 16) and then , It may be preferred to feed the combined flow as a single feed to the lower region of the absorber 118c.

If the feed gas is richer, the amount of liquid separated in stream 35 is between expanded stream 39a and expanded liquid stream 40a shown in FIGS. 3, 7, 11, and 15, or expanded flow. It may be large enough to prefer to place an additional mass transfer zone of the demethanizer 118d between 34a and the expanded liquid stream 40a shown in FIGS. 5, 9, 13, and 17. In such a case, the heat and mass transfer means of the demethanizer 118d can be configured in the upper part and the lower part so that the expanded liquid stream 40a can be introduced between the two parts. As indicated by the dashed line, in some situations, a portion of the liquid stream 35 (stream 37) is vaporized in the stream 36 (FIGS. 3, 7, 11 and 15), or cooled first. It may be preferred to combine with the second portion 33a (FIGS. 5, 9, 13, 17) to form a combined flow 38. On the other hand, the remaining part of the liquid stream 35 (stream 40) is expanded to reduce the pressure and is supplied as a stream 40a between the upper and lower parts of the heat and mass transfer means of the demethanizer 118d.

  In some situations, the cooled first and second portions (flows 32a and 33a shown in FIGS. 4, 5, 8, 9, 12, 13, 16, and 17). ) May not be preferred. In such a case, only the cooled first portion 32a is the separator portion 118e within the processing assembly 118 (FIGS. 4, 5, 12, and 13), or the vapor (stream 34) is a concentrated liquid (stream 35). ) From the separator 12 (FIGS. 8, 9, 16, and 17) separated from the The vapor stream 34 enters the work expander 15 and is expanded substantially isentropically to the operating pressure of the absorber 118 c so that the expanded stream 34 a is in the lower region of the absorber 118 c inside the processing assembly 118. Supplied as a feed. The cooled second portion 33 a is combined with the separated liquid (stream 35 via stream 37), and the combined stream 38 is a heat exchange means in the lower region of the feed cooling section 118 a inside the processing assembly 118. And cooled to a substantial concentrate. Substantially concentrated stream 38a is flash expanded through expansion valve 14 to the operating pressure of absorber 118c, so that expanded stream 38b is supplied to separator portion 118b within processing assembly 118. In some situations, only a portion of the liquid stream 35 (stream 37) is combined with the cooled second portion 33a, and the remaining portion (stream 40) passes through the expansion valve 17 to the bottom of the absorber 118c. It may be preferred to be supplied to the area. In other situations, it may be preferred to send all of the liquid flow 35 through the expansion valve 17 to the lower region of the absorber 118c.

  In some situations, it may be advantageous to use an external separator vessel to separate the cooled feed stream 31a or the cooled first portion 32a, rather than including the separator portion 118e in the processing assembly 118. Sometimes. A separator 12 may be used to separate the cooled feed stream 31a into a vapor stream 34 and a liquid stream 35, as shown in FIGS. Similarly, as shown in FIGS. 8, 9, 16, and 17, the separator 12 can be used to separate the cooled first portion 32 a into a vapor stream 34 and a liquid stream 35.

  Depending on the amount of heavier hydrocarbons in the feed gas and the pressure of the feed gas, the separator portion 118e of FIGS. 2, 3, 10, and 11, or FIGS. 6, 7, 14, and The separator 12 of FIG. 15 (the cooled first portion 32a entering the separator portion 118e of FIGS. 4, 5, 12, and 13 or the separator 12 of FIGS. 8, 9, 16, and 17). The cooled feed stream 31a entering) may not contain any liquid (because it is above its dew point or because it is above its cricon denvar). In such a case, streams 35 and 37 (shown in dashed lines) are free of liquid, and therefore vapor from separator portion 118e in stream 36 (FIGS. 2, 3, 10, and 11), stream 36 (FIG. 6, 7, 14, and 15), or the cooled second portion 33 a (FIGS. 4, 5, 8, 9, 12, 13, and 16). , And FIG. 17) flow to stream 38, resulting in an expanded substantially concentrated stream 38b that is fed to separator portion 118b in processing assembly 118. In such a situation, the separator portion 118e of the processing assembly 118 (FIGS. 2-5 and 10-13) or the separator 12 (FIGS. 6-9 and 14-17) may not be required. .

Supply gas conditions, plant size, available equipment, or other factors can be eliminated by the work expander 15 or replaced with an alternative expansion device (such as an expansion valve). Individual flow expansions are shown for specific expansion devices, but alternative expansion means may be utilized where appropriate. For example, the condition may justify work expansion of a substantially concentrated portion of the feed stream (stream 38a).

In accordance with the present invention, the use of external cooling to supplement the cooling available to the inlet vapor from the distilled vapor and liquid streams may be utilized particularly in the case of inlet rich gases. In such a case, the heat and mass transfer means may be configured such that the separator portion 118e (or the cooled feed stream 31a or the cooled first portion 32a shown in FIG. 2 to FIG. 5 and FIG. 10 to FIG. Gas collecting means in such cases when not included) or heat and mass transfer means may be included in the separator 12 indicated by broken lines in FIGS. 6-9 and 14-17. This heat and mass transfer means may be other types of heat transfer including fin and tube heat exchangers, plate heat exchangers, brazed aluminum heat exchangers, or multi-pass and / or multi-service heat exchangers It can consist of devices. The heat and mass transfer means includes a coolant flow (eg, propane) and a flow 31a (FIGS. 2, 3, 6, 7, 10, 11, 11) that flow through one flow path of the heat and mass transfer means. 14 and 15) or an upward flow 32a (FIGS. 4, 5, 8, 9, 12, 12, 13, 16 and 17) to achieve heat exchange. Thus, the coolant further cools the vapor and falls down, concentrating additional liquid that becomes part of the liquid removed in stream 25. Alternatively, a conventional gas cooling device (s) may be used where the flow 31a is separated by the separator portion 118e (FIGS. 2, 3, 10, and 11) or the separator 12 (FIGS. 6, 7, 14). , And FIG. 15) or the flow 32a enters the separator portion 18e (FIGS. 4, 5, 12, and 13) or the separator 12 (FIGS. 8, 9, 16, and 17). Could be used to cool stream 32a, stream 33a, and / or stream 31a with coolant.

Temperature and rich feed gas, and in accordance with the amount of C ₂ components are recovered in the liquid product stream 44, the liquid leaving the demethanizer unit 118d enough to meet product specifications sufficient heating is not available from the stream 33 Sometimes. In such a case, the heat and mass transfer means of the demethanizer 118d may include provisions for providing supplemental heating with the heating medium indicated by the dashed lines in FIGS. Alternatively, another heat and mass transfer means can be included in the lower region of the demethanizer 118d to provide supplemental heating, or the stream 33 can be heat and material in the demethanizer 118d. It can be heated with a heating medium before being supplied to the moving means.

Depending on the type of heat transfer device selected for heat exchange means in the upper and lower regions of the feed cooler 118a, these heat exchanges within a single multi-pass device and / or multi-service heat transfer device It may be possible to combine means. In such a case, the multi-pass device and / or multi-service heat transfer device may be used to disperse, separate, and collect stream 32, stream 38, and distillation vapor stream to achieve the desired cooling and heating. Including appropriate means.

In some situations, it may be preferred to achieve additional mass transfer within the upper region of the demethanizer 118d. In such a case, the mass transfer means may include the expansion flow 39a (FIGS. 2, 3, 6, 7, 10, 10, 11, and 15) or the expansion flow 34a (FIGS. 4, 5, and 8). 9, FIG. 12, FIG. 13, FIG. 16, and FIG. 17) enter the lower region of the absorber 118 c and the cooled second portion 33 a is a heat and mass transfer means in the demethanizer 118 d. Can be placed above and away.

A less preferred option of the embodiments of FIGS. 2, 3, 6, 7, 10, 11, 14, and 15 of the present invention is the separator container for the cooled first portion 32a. Providing a separator vessel for the cooled second portion 33a, combining the vapor streams separated therein to form vapor stream 34, and being separated therein to form liquid stream 35. The combined liquid flow. Another less preferred option of the present invention is that rather than combining stream 37 with stream 36 or stream 33a to form combined stream 38 , FIG. 2, FIG. 3, FIG. 4, FIG. 7, 8, and 9 in separate heat exchange means within the feed cooling section 118 a , or in FIGS. 10, 11, 12, 13, 14, 15, 16, and 17. The flow 37 is cooled in a separate passage in the heat exchanger 10, the cooled flow is expanded in a separate expansion device, and the expanded flow is supplied to an intermediate region in the absorber 118c.

  The relative amount of feed found in each branch of the split steam feed depends on several factors including gas pressure, feed gas composition, the amount of heat that can be economically extracted from the feed, and the amount of horsepower available. It is recognized that it depends. More feed above the absorber 118c may increase recovery while reducing the power recovered from the expander, thereby increasing recompression horsepower requirements. Increasing the feed below the absorber 118c reduces horsepower consumption but may also reduce product recovery.

The present invention relates to the recovery of C ₂ component, C ₃ component, and heavier hydrocarbon components, or C ₃ component and heavier hydrocarbons per utility cost required to operate the process. Achieve improved component recovery. Improvements in utility costs required to operate the process manifest in the form of reduced power requirements for compression or recompression, reduced power requirements for external cooling, reduced energy requirements for supplemental heating, or a combination thereof Sometimes.

  Although described as considered to be preferred embodiments of the invention, those skilled in the art will recognize, for example, feed the invention without departing from the spirit of the invention as defined by the following claims. It will be appreciated that other and additional modifications may be made to it, such as adapting to various conditions, types, or other requirements.

Claims (22)

A gas stream ( 31 ) containing methane, C ₂ component, C ₃ component, and heavier hydrocarbon component is separated into a volatile residual gas fraction ( 4ld ) and most of the C ₂ component, the C most of the _three components, and most or containing, or most of the C ₃ minutes hydrocarbon components heavier than the, and relatively containing a large portion of the hydrocarbon components heavier than the A process for separating into fractions of low volatility ( 44 ) ,
(1) dividing the gas stream ( 31 ) into a first part ( 32 ) and a second part ( 33 ) ;
(2) cooling the first portion ( 32 ) (10);
(3) cooling the second part ( 33 ) (118d);
(4) the cooled first portion ( 32a ) and the cooled second portion ( 33a ) are merged to form a cooled gas stream ( 31a, 34 ) ;
(5) dividing the cooled gas stream ( 31a, 34 ) into a first stream ( 36 ) and a second stream ( 39 ) ;
(6) said first stream (36) and cooling (10), its substantial all condensed (38a), followed by more in low pressure to Rise Zhang (14) and further cooled (38b ),
(7) supplying the expanded and cooled first stream as a top feed ( 38b ) to an absorbent means ( 118c ) contained in a processing assembly ( 118 ) ;
(8) the second stream ( 39 ) is expanded to a lower pressure (15) and fed as a bottom feed ( 39a ) to the absorption means ( 118c ) ;
(9) The distillation vapor stream ( 41 ) is collected from the upper region of the absorption means ( 118c ) and heated in one or more heat exchange means ( 10 ) , thereby providing steps (2) and (6) Supplying at least a part of the cooling of the product, followed by discharging the heated distilled steam stream ( 41a ) as the volatile residual gas fraction (41d) ,
(10) Collect a distilled liquid stream from the lower region of the absorption means ( 118c ) and heat in the heat and mass transfer means ( 118d ) contained in the processing assembly ( 118 ) , thereby providing step (3) Simultaneously stripping the higher volatile components exiting the distillation liquid stream while supplying at least a portion of the cooling in, followed by the heating stripped distillation liquid stream to the relatively volatile Discharged from the processing assembly ( 118 ) as a low fraction ( 44 ) ,
(11) the quantity and temperature, the temperature as a majority of the components of the relatively less volatile fraction (44) in is recovered in the relative absorption means (118c) feed stream (38b, 39a) is effective <br/> method for the maintaining the temperature of the upper region of the absorption means (118c) to.   Methane, C ₂ Ingredient C ₃ Component, and a gas stream (31) containing a heavier hydrocarbon component, a volatile residual gas fraction (4ld), and said C ₂ Most of the ingredients, said C ₃ Contains most of the components and most of the heavier hydrocarbon components or the C ₃ And a relatively low volatility fraction (44) containing a majority of the water and a majority of the heavier hydrocarbon component comprising:
  (1) dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) cooling the first part (32) (10);
  (3) cooling the second part (33) (118d);
  (4) The cooled first portion (32a) and the cooled second portion (33a) merge to form a partially condensed gas stream (31a);
  (5) The partially condensed gas stream (31a) is fed to a separation means (12 or 118e) and separated therein to provide a vapor stream (34) and at least one liquid stream (35) And
  (6) dividing the steam stream (34) into the first stream (36) and the second stream (39);
  (7) Cool (10) the first stream (36), condense substantially all of it (38a), then expand to a lower pressure (14), further cool (38b),
  (8) supplying the expanded and cooled first stream as a top feed (38b) to an absorbent means (118c) contained in a processing assembly (118);
  (9) the second stream (39) is expanded to a lower pressure (15) and fed as a bottom feed (39a) to the absorption means (118c);
  (10) inflating (17) at least a portion (40) of said at least one liquid stream (35) to said lower pressure;
    (10a) supplying (40a) the expanded at least part of the at least one liquid stream as a second bottom feed to the absorbing means (118c), or
    (10b) (i) the heat and mass transfer means (118d) has upper and lower regions;
            (Ii) the processing assembly (118) such that the expanded at least part of the at least one liquid stream enters between the upper and lower regions of the heat and mass transfer means (118d). (40a),
  (11) The distillation vapor stream (41) is collected from the upper region of the absorption means (118c) and heated in one or more heat exchange means (10), thereby providing steps (2) and (7) Supplying at least a part of the cooling of the gas, followed by discharging the heated distilled steam stream (41a) as the volatile residual gas fraction (41d),
  (12) Collect a distilled liquid stream from the lower region of the absorption means (118c) and heat it in the heat and mass transfer means (118d) contained in the processing assembly (118), thereby providing a step (3 ) Simultaneously stripping the higher volatile components exiting the distillation liquid stream while supplying at least a portion of the cooling in), followed by the heating and stripping distillation liquid stream to the relatively volatile Discharging from the processing assembly (118) as a fraction of low character (44);
  (13) The amount and temperature of the feed stream (38b, 39a, 40a) relative to the absorption means (118c) is such that most of the components in the relatively volatile fraction (44) are recovered. Effective to maintain the temperature of the upper region of the absorption means (118c) at a certain temperature.
Method.   Methane, C ₂ Ingredient C ₃ Component, and a gas stream (31) containing a heavier hydrocarbon component, a volatile residual gas fraction (4ld), and said C ₂ Most of the ingredients, said C ₃ Contains most of the components and most of the heavier hydrocarbon components or the C ₃ And a relatively low volatility fraction (44) containing a majority of the water and a majority of the heavier hydrocarbon component comprising:
  (1) dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) cooling the first part (32) (10);
  (3) cooling the second part (33) (118d);
  (4) The cooled first portion (32a) and the cooled second portion (33a) merge to form a partially condensed gas stream (31a);
  (5) The partially condensed gas stream (31a) is fed to a separation means (12 or 118e) and separated therein to provide a vapor stream (34) and at least one liquid stream (35) And
  (6) dividing the steam stream (34) into the first stream (36) and the second stream (39);
  (7) merging the first stream (36) with at least a portion (37) of the at least one liquid stream (35) to form a merged stream (38);
  (8) The combined stream (38) is cooled (10) and substantially all condensed (38a) and subsequently expanded to a lower pressure (14), thereby further cooling ( 38b),
  (9) supplying the expanded and cooled combined stream (38b) as the top feed to an absorbent means (118c) contained in a processing assembly (118);
  (10) expanding the second stream (39) to the lower pressure (15) and supplying it as a first bottom feed (39a) to the absorption means (118c);
  (11) expanding any remaining portion (40) of the at least one liquid stream (35) to the lower pressure (17);
        (11a) supplying (40a) the optional expanded portion of the at least one liquid stream as a second bottom feed to the absorption means (118c), or
        (11b) (i) the heat and mass transfer means (118d) has upper and lower regions;
                  (Ii) the processing assembly (118) such that any remaining expanded portion of the at least one liquid stream enters between the upper and lower regions of the heat and mass transfer means (118d). ) (40a)
  (12) The distillation vapor stream (41) is collected from the upper region of the absorption means (118c) and heated in one or more heat exchange means (10), thereby providing steps (2) and (8) Supplying at least a part of the cooling of the gas, followed by discharging the heated distilled steam stream (41a) as the volatile residual gas fraction (41d),
  (13) A distilled liquid stream is collected from the lower region of the absorption means (118c) and heated in the heat and mass transfer means (118d) contained in the processing assembly (118), whereby step (3 ) Simultaneously stripping the higher volatile components exiting the distillation liquid stream while supplying at least a portion of the cooling in), followed by the heating and stripping distillation liquid stream to the relatively volatile Discharging from the processing assembly (118) as a fraction of low character (44);
  (14) The amount and temperature of the feed stream (38b, 39a, 40a) relative to the absorption means (118c) is such that most of the components in the relatively volatile fraction (44) are recovered. Effective to maintain the temperature of the upper region of the absorption means (118c) at a certain temperature.
Method.   Methane, C ₂ Ingredient C ₃ Component, and a gas stream (31) containing a heavier hydrocarbon component, a volatile residual gas fraction (4ld), and said C ₂ Most of the ingredients, said C ₃ Contains most of the components and most of the heavier hydrocarbon components or the C ₃ And a relatively low volatility fraction (44) containing a majority of the water and a majority of the heavier hydrocarbon component comprising:
  (1) dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) Cool (10) the first part (32) and then expand to the low pressure (15);
  (3) supplying the expanded and cooled first portion (34a) as the bottom feed to an absorbent means (118c) contained in a processing assembly (118);
  (4) The second part (33) is cooled (118d, 10), all of which is substantially condensed (38a) and subsequently expanded to the low pressure (14), further cooling. (38b),
  (5) supplying the expanded and cooled second portion (38b) as the top feed to the absorbing means (118c);
  (6) The distillation vapor stream (41) is collected from the upper region of the absorption means (118c) and heated in the one or more heat exchange means (10), thereby providing steps (2) and ( Supplying at least a portion of the cooling in 4), followed by discharging the heated distillation vapor stream (41a) as the volatile residual gas fraction (41d),
  (7) The distillation vapor stream is collected from the lower region of the absorption means (118c) and heated in heat and mass transfer means (118d) contained in the processing assembly (118), thereby providing a step ( 4) simultaneously stripping higher volatile components exiting the distillation liquid stream while supplying at least a portion of the cooling in 4), followed by the heating and stripping distillation liquid stream relative to the Discharged from the processing assembly (118) as a low volatility fraction (44);
  (8) The amount and temperature of the feed stream (38b, 34a) relative to the absorption means (118c) is such that most of the components in the relatively volatile fraction (44) are recovered. Effective to maintain the temperature of the upper region of the absorbing means (118c)
Method.   Methane, C ₂ Ingredient C ₃ Component, and a gas stream (31) containing a heavier hydrocarbon component, a volatile residual gas fraction (4ld), and said C ₂ Most of the ingredients, said C ₃ Contains most of the components and most of the heavier hydrocarbon components or the C ₃ And a relatively low volatility fraction (44) containing a majority of the water and a majority of the heavier hydrocarbon component comprising:
  (1) dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) the first part (32) is sufficiently cooled (10) and partially condensed (32a);
  (3) supplying said partially condensed first part (32a) to a separation means (12 or 118e) and separating therein, vapor stream (34) and at least one liquid stream (35); Offer to,
  (4) expanding (15) the vapor stream (34) to a lower pressure and supplying it as a first bottom feed (34a) to an absorbent means (118c) contained in the processing assembly (118);
  (5) expanding at least a portion (40) of the at least one liquid stream (35) to the lower pressure;
        (5a) supplying the expanded at least part of the at least one liquid stream as a second bottom feed (40a) to the absorption means (118c), or
        (5b) (i) the heat and mass transfer means (118d) has upper and lower regions;
                (Ii) the processing assembly (118) such that the expanded at least part of the at least one liquid stream enters between the upper and lower regions of the heat and mass transfer means (118d). (40a),
  (6) The second part (33) is cooled (118d, 10), all of which is substantially condensed (38a) and subsequently expanded to the low pressure (14), further cooling. (38b),
  (7) supplying the expanded and cooled second portion (38b) as the top feed to the absorbing means (118c);
  (8) A distilled vapor stream (41) is collected from the upper region of the absorption means (118c) and heated in the one or more heat exchange means (10), thereby providing steps (2) and (6) At least a portion of the cooling in), followed by discharging the heated distilled steam stream (41a) as the volatile residual gas fraction (41d),
  (9) A distilled vapor stream is collected from the lower region of the absorption means (118c) and heated in the heat and mass transfer means (118d) contained in the processing assembly (118), thereby providing a step ( Simultaneously stripping higher volatile components exiting the distillation liquid stream while providing at least a portion of the cooling in 6), followed by the heating and stripping distillation liquid stream relative to the Discharged from the processing assembly (118) as a low volatility fraction (44);
  (10) The amount and temperature of the feed stream (38b, 39a, 40a) relative to the absorption means (118c) is such that most of the components in the relatively volatile fraction (44) are recovered. Effective to maintain the temperature of the upper region of the absorption means (118c) at a certain temperature.
Method.   Methane, C ₂ Ingredient C ₃ Component, and a gas stream (31) containing a heavier hydrocarbon component, a volatile residual gas fraction (4ld), and said C ₂ Most of the ingredients, said C ₃ Contains most of the components and most of the heavier hydrocarbon components or the C ₃ And a relatively low volatility fraction (44) containing a majority of the water and a majority of the heavier hydrocarbon component comprising:
  (1) dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) the first part (32) is sufficiently cooled (10) and partially condensed (32a);
  (3) supplying said partially condensed first part (32a) to a separation means (12 or 118e) and separating therein, vapor stream (34) and at least one liquid stream (35); Offer to,
  (4) expanding (15) the vapor stream (34) to a lower pressure and supplying it as a first bottom feed (34a) to an absorbent means (118c) contained in the processing assembly (118);
  (5) Cool (118d) the second part (33) and then merge with at least a portion (37) of the at least one liquid stream (35) to form a merged stream (38). ,
  (6) Cool the combined stream (38) (10), substantially condense it all (38a), and then expand to the lower pressure (14), thereby further cooling ( 38b),
  (7) supplying the expanded and cooled combined stream (38b) as a top feed to the absorption means (118c);
  (8) expanding any remaining portion (40) of the at least one liquid stream (35) to the lower pressure (17);
        (8a) supplying any remaining expanded portion of the at least one liquid stream as a second bottom feed (40a) to the absorption means (118c), or
        (8b) (i) the heat and mass transfer means (118d) has upper and lower regions;
                (Ii) the processing assembly (118) such that any remaining expanded portion of the at least one liquid stream enters between the upper and lower regions of the heat and mass transfer means (118d). ) (40a)
  (9) A distilled vapor stream (41) is collected from the upper region of the absorption means (118c) and heated in the one or more heat exchange means (10), thereby providing steps (2) and (6) At least a portion of the cooling in), followed by discharging the heated distilled steam stream (41a) as the volatile residual gas fraction (41d),
  (10) A distilled vapor stream is collected from the lower region of the absorption means (118c) and heated in the heat and mass transfer means (118d) contained in the processing assembly (118), thereby providing a step ( 5) simultaneously stripping higher volatile components exiting the distillation liquid stream while supplying at least a portion of the cooling in step 5), followed by the heating and stripping distillation liquid stream relative to the Discharged from the processing assembly (118) as a low volatility fraction (44);
  (11) The amount and temperature of the feed stream (38b, 39a, 40a) relative to the absorption means (118c) is such that most of the components in the relatively volatile fraction (44) are recovered. Effective to maintain the temperature of the upper region of the absorption means (118c) at a certain temperature.
Method. The method of claim 2, 3, 5, or 6 , wherein said separating means ( 118e ) is housed in said processing assembly ( 118 ) . (1) housing the gas collection means ( 118e ) in the processing assembly ( 118 ) ;
(2) additional heat and mass transfer means including one or more paths leading to an external cooling medium are included within the gas collection means ( 118e ) ;
(3) supplying the cooled gas stream ( 31a ) to the gas collecting means ( 118e ) and leading to the additional heat and mass transfer means further cooled by the external cooling medium;
(4) dividing the further cooled gas stream ( 34 ) into the first stream ( 36 ) and the second stream ( 39 ) ;
The method of claim 1. (1) housing the gas collection means ( 118e ) in the processing assembly ( 118 ) ;
(2) additional heat and mass transfer means including one or more paths leading to an external cooling medium are included within the gas collection means ( 118e ) ;
(3) supplying the cooled first portion ( 32a ) to the gas collection means ( 118e ) and leading to the additional heat and mass transfer means further cooled by the external cooling medium;
(4) The further cooled first portion ( 34 ) is expanded to a lower pressure (15) and subsequently fed to the absorption means ( 118c ) as the bottom feed ( 34a).
The method of claim 4. (1) including additional heat and mass transfer means including one or more paths leading to an external cooling medium within the separation means ( 12 or 118e) ;
(2) directing the vapor stream to the additional heat and mass transfer means cooled by the external cooling medium to form additional condensate;
(3) the condensate, a part of the separated in its This at least one liquid stream (35),
The method of claim 2, 3, 5, 6, was or 7. The heat and mass transfer means ( 118d ) provides an external heating medium that supplements the heating supplied by the feed gas ( 33 ) for stripping the higher volatile components exiting the distillation liquid stream. Contains one or more routes to go through,
The method of claim 6, 7, 8, 9 or 1 0,. A gas stream ( 31 ) containing methane, C ₂ component, C ₃ component and heavier hydrocarbon component is separated from the volatile residual gas fraction ( 41d ) and most of the C ₂ component, the C ₃ most of the components, and either contains most of the hydrocarbon components heavier than the, or relatively containing the majority, and most of the hydrocarbon components heavier than the said C ₃ components An apparatus for separating into fractions of low volatility ( 44 ) ,
(1) a first dividing means for dividing said gas stream (31) into a first portion (32) and a second portion (33),
(2) first heat exchange means ( 10 ) connected to the first dividing means for receiving and cooling the first part ( 32 ) ;
(3) a heat and mass transfer means ( 118d ) connected to the first dividing means and received in the processing assembly ( 118 ) for receiving and cooling the second part ( 33 ) ;
(4) connected to the first heat exchange means ( 10 ) and the heat and mass transfer means ( 118d ) , the cooled first part ( 32a ) and the cooled second part ( 33a ) and a merging means for forming a cooled gas stream ( 31a, 34 ) ;
(5) a second division connected to the merging means and receiving the cooled gas stream ( 31a, 34 ) and dividing it into a first stream ( 36 ) and a second stream ( 39 ) Means,
(6) the second is connected to the dividing means, the first receiving the stream (36) of which substantially condenses (38a) as in the second heat exchange means to sufficiently cool (10 ) And
(7) the is connected to the second heat exchange means (10), the receiving substantially condensed first stream (38a), to inflate it to a lower pressure (38b) first Expansion means ( 14 ) ;
(8) is housed in said processing assembly (118), the first connected to the expansion means (14), receiving a first stream being cooled by the expansion of the top feed (38b) thereto Absorption means ( 118c ) ;
(9) the is connected to a second dividing means, receiving said second stream (39), an inflating said from the low pressure (39a) second expansion means (15), said absorbent and further connected to means (118c), as the bottom feed thereto, said supplying a second stream is expanded (39a), and a second expansion means (15),
(10) the processing is housed in the assembly (118), connected to said absorbing means (118c), the vapor collection means for receiving a distillation vapor stream from an upper region of said absorbent means (118c) and (118b),
(11) further connected to the steam collecting means ( 118b ) for receiving and heating the distilled steam stream ( 41 ) , thereby providing at least part of the cooling of the step (6), Heat exchange means ( 10 ) ;
(12) further connected to the second heat exchange means ( 10 ) to receive and heat the heated distillation vapor stream, thereby supplying at least a part of the cooling of the step (2) Followed by the first heat exchange means ( 10 ) for discharging the further heated distilled steam stream ( 41a ) as the volatile residual gas fraction (41d) ;
(13) liquid collection means connected to the absorption means ( 118c ) and contained in the processing assembly ( 118 ) for receiving a distilled liquid stream from a lower region of the absorption means ( 118c ) ;
(14) further connected to the liquid collecting means, receiving the distilled liquid stream, heating it and supplying at least part of the cooling in step (3) higher than exiting the distilled liquid stream volatile components were stripped simultaneously, subsequently, the heat releasing distillation liquid stream wherein the heating is stripped from said processing assembly as relatively less volatile fraction (44) (118) And mass transfer means ( 118d ) ;
(15) the feed stream (38b, 39a) to said absorbing means (118c) tweezers adjusting the amount and temperature of the majority of the components of the relatively volatile in low fraction (44) is recovered And control means for maintaining the temperature of the upper region of the absorption means ( 118c ) at such a temperature.   Methane, C ₂ Ingredient C ₃ The gas stream (31) containing the components and the heavier hydrocarbon component, the volatile residual gas fraction (41d) and the C ₂ Most of the ingredients, said C ₃ Contains most of the components, and most of the heavier hydrocarbon components, or the C ₃ An apparatus for separating a majority of the components and a relatively less volatile fraction (44) containing a majority of the heavier hydrocarbon components,
  (1) first dividing means for dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) first heat exchange means (10) connected to the first dividing means for receiving and cooling the first part (32);
  (3) a heat and mass transfer means (118d) connected to the first dividing means and received in the processing assembly (118) for receiving and cooling the second part (33);
  (4) connected to the first heat exchange means (10) and the heat and mass transfer means (118d), the cooled first part (32a) and the cooled second part ( A confluence means for receiving 33a) and forming a partially condensed gas stream (31a);
  (5) Separation means (12 or 12) connected to the merging means for receiving the partially condensed gas stream (31a) and separating it into a vapor stream (34) and at least one liquid stream (35). 118e)
  (6) a second division connected to the separation means (12 or 118e) and accepting the vapor stream (34) and dividing it into a first stream (36) and a second stream (39) Means,
  (7) second heat exchange means (10) connected to the second dividing means and receiving the first stream (36) and cooling it sufficiently to substantially condense (38a). )When,
  (8) connected to the second heat exchange means (10) and accepts the substantially condensed first stream (38a) and expands it to a lower pressure (38b) first expansion Means (14);
  (9) Housed in the processing assembly (118) and connected to the first expansion means (14) to receive the expanded and cooled first stream (38b) as a top feed thereto Absorption means (118c);
  (10) Second expansion means (15) connected to the second dividing means and receiving the second stream (39) and expanding it to the lower pressure (39a), wherein the absorbing means A second expansion means (15) further connected to (118c) and supplying said expanded second stream (39a) as a first bottom feed thereto;
  (11) Third expansion means (17) connected to the separation means (12 or 118e), accepts at least a portion (40) of the at least one liquid stream (35) and expands to the lower pressure. Because
        (11a) further connected to said absorbing means (118c) to supply said expanded liquid stream (40a) as a second bottom feed thereto, or
        (11b) (i) the heat and mass transfer means (118d) has upper and lower regions;
                (Ii) connecting said processing assembly (118) to said third expansion means (17) to receive said expanded at least part of said at least one liquid stream (40a), said heat and mass transfer means; Leading between said upper and lower regions of (118d),
Said third expansion means (17);
  (12) steam collecting means (118b) housed in the processing assembly (118), connected to the absorbing means (118c) and receiving a distilled steam stream from an upper region of the absorbing means (118c);
  (13) further connected to the steam collecting means (118b) for receiving and heating the distilled steam stream (41), thereby providing at least a portion of the cooling of the step (7); Heat exchange means (10);
  (14) further connected to the second heat exchange means (10) to receive and heat the heated distillation vapor stream, thereby supplying at least a portion of the cooling of the step (2). Followed by the first heat exchange means (10) for releasing the further heated distillation vapor stream (41a) as the volatile residual gas fraction (41d);
  (15) liquid collection means connected to the absorption means (118c) and contained in the processing assembly (118) for receiving a distilled liquid stream from the lower region of the absorption means (118c);
  (16) further connected to the liquid collecting means, receiving the distilled liquid stream, heating it and supplying at least part of the cooling in step (3), higher than coming out of the distilled liquid stream The heat that simultaneously strips volatile components and then releases the heated stripped distilled liquid stream from the processing assembly (118) as the relatively less volatile fraction (44). And mass transfer means (118d);
  (17) Adjusting the amount and temperature of the feed stream (38b, 39a, 40a) to the absorption means (118c) to recover most of the components in (44) in the relatively volatile fraction. Control means for maintaining the temperature of the upper region of the absorption means (118c) at such a temperature;
Equipped with the device.   Methane, C ₂ Ingredient C ₃ The gas stream (31) containing the components and the heavier hydrocarbon component, the volatile residual gas fraction (41d) and the C ₂ Most of the ingredients, said C ₃ Contains most of the components, and most of the heavier hydrocarbon components, or the C ₃ An apparatus for separating a majority of the components and a relatively less volatile fraction (44) containing a majority of the heavier hydrocarbon components,
  (1) first dividing means for dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) first heat exchange means (10) connected to the first dividing means for receiving and cooling the first part (32);
  (3) a heat and mass transfer means (118d) connected to the first separation means and received in the processing assembly (118) for receiving and cooling the second part (33);
  (4) connected to the first heat exchange means (10) and the heat and mass transfer means (118d), the cooled first part (32a) and the cooled second part ( 33a) a first confluence means for receiving and forming a partially condensed gas stream (31a);
  (5) Separation means connected to the first merge means for receiving the partially condensed gas stream (31a) and separating it into a vapor stream (34) and at least one liquid stream (35). (12 or 118e),
  (6) a second division connected to the separation means (12 or 118e) and accepting the vapor stream (34) and dividing it into a first stream (36) and a second stream (39) Means,
  (7) connected to the second dividing means and the separating means (12 or 118e), and at least a part (37) of the first stream (36) and the at least one liquid stream (35) A second joining means for forming a receiving and joining stream (38);
  (8) Second heat exchange means (10) connected to the second merging means and receiving the merged stream (38) and cooling it sufficiently to condense it substantially (38a). When,
  (9) connected to the second heat exchange means (10) and accepts the substantially condensed merged stream (38a) and expands it to a lower pressure (38b) first expansion means ( 14)
  (10) Absorption contained in the processing assembly (118) and connected to the first expansion means (14) to receive the expanded and cooled combined stream (38b) as a top feed thereto Means (118c);
  (11) Connected to the second dividing means, accepts the second stream (39) and expands it to the lower pressure (39a) Second expanding means (15), the absorbing means A second expansion means (15) further connected to (118c) and supplying said expanded second stream (39a) as a first bottom feed thereto;
  (12) connected to the separation means (12 or 118e) and accepts any remaining portion (40) of the at least one liquid stream (35) and expands to the lower pressure (40a) a third Expansion means (17),
        (12a) further connected to the absorbing means (118c) to supply the expanded liquid stream (40a) as a second bottom feed thereto, or
        (12b) (i) the heat and mass transfer means (118d) has upper and lower regions;
                  (Ii) connecting the processing assembly (118) to the third expansion means (17) to receive any remaining expanded portion of the at least one liquid stream (40a); Leading between said upper and lower regions of moving means (118d),
Said third expansion means (17);
  (13) a steam collecting means (118b) housed in the processing assembly (118), connected to the absorbing means (118c) and receiving a distilled steam stream from an upper region of the absorbing means (118c);
  (14) further connected to the steam collecting means (118b) for receiving and heating the distilled steam stream (41), thereby providing at least a portion of the cooling of the step (8), Heat exchange means (10);
  (15) further connected to the second heat exchange means (10) for receiving and heating the heated distillation vapor stream, thereby supplying at least a portion of the cooling of the step (2). Followed by the first heat exchange means (10) for releasing the further heated distillation vapor stream (41a) as the volatile residual gas fraction (41d);
  (16) liquid collection means connected to the absorption means (118c) and contained in the processing assembly (118) for receiving a distilled liquid stream from a lower region of the absorption means (118c);
  (17) further connected to the liquid collecting means, receiving the distilled liquid stream, heating it and supplying at least part of the cooling in step (3), higher than coming out of the distilled liquid stream The heat that simultaneously strips volatile components and then releases the heated stripped distilled liquid stream from the processing assembly (118) as the relatively less volatile fraction (44). And mass transfer means (118d);
  (18) Adjusting the amount and temperature of the feed stream (38b, 39a, 40a) relative to the absorption means (118c), most of the components in the relatively volatile fraction (44) are recovered. Control means for maintaining the temperature of the upper region of the absorption means (118c) at such a temperature;
Equipped with the device.   Methane, C ₂ Ingredient C ₃ The gas stream (31) containing the components and the heavier hydrocarbon component, the volatile residual gas fraction (41d) and the C ₂ Most of the ingredients, said C ₃ Contains most of the components, and most of the heavier hydrocarbon components, or the C ₃ An apparatus for separating a majority of the components and a relatively less volatile fraction (44) containing a majority of the heavier hydrocarbon components,
  (1) dividing means for dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) first heat exchange means (10) connected to said dividing means for receiving said first part (32) and cooling it;
  (3) a heat and mass transfer means (118d) connected to the dividing means and received in the processing assembly (118) for receiving and cooling the second part (33);
  (4) connected to the heat and mass transfer means (118d), accepts the cooled second portion (33a), further cools and substantially condenses (38a) a second Heat exchange means (10);
  (5) connected to the second heat exchange means (10) and accepts the substantially condensed second part (38a) and expands it to a lower pressure (38b) first expansion Means (14);
  (6) Housed in the processing assembly (118) and connected to the first expansion means (14) to receive the expanded and cooled second portion (38b) as a top feed thereto Absorption means (118c);
  (7) Connected to the first heat exchange means (10), accepts the cooled first part (32a) and expands it to a lower pressure (34a) with second expansion means (15) Second expansion means (15), further connected to said absorption means (118c) and supplying said expanded and cooled first stream (34a) as a bottom feed thereto;
  (8) a steam collecting means (118b) housed in the processing assembly (118), connected to the absorbing means (118c) and receiving a distilled steam stream from an upper region of the absorbing means (118c);
  (9) further connected to the steam collecting means (118b) for receiving and heating the distilled steam stream (41), thereby providing at least part of the cooling of the step (4), Heat exchange means (10);
  (10) further connected to the second heat exchange means (10) to receive and heat the heated distillation vapor stream, thereby supplying at least a portion of the cooling of the step (2). Followed by the first heat exchange means (10) for releasing the further heated distillation vapor stream (41a) as the volatile residual gas fraction (41d);
  (11) liquid collection means connected to the absorption means (118c) and contained in the processing assembly (118) for receiving a distilled liquid stream from a lower region of the absorption means (118c);
  (12) further connected to the liquid collection means, receiving the distilled liquid stream, heating it and supplying at least part of the cooling in step (3), higher than coming out of the distilled liquid stream The heat that simultaneously strips volatile components and then releases the heated stripped distilled liquid stream from the processing assembly (118) as the relatively less volatile fraction (44). And mass transfer means (118d);
  (13) Adjust the amount and temperature of the feed stream (38b, 39a) to the absorption means (118c) so that most of the components in the relatively volatile fraction (44) are recovered. Control means for maintaining the temperature of the upper region of the absorption means (118c) at a certain temperature;
Equipped with the device.   Methane, C ₂ Ingredient C ₃ The gas stream (31) containing the components and the heavier hydrocarbon component, the volatile residual gas fraction (41d) and the C ₂ Most of the ingredients, said C ₃ Contains most of the components, and most of the heavier hydrocarbon components, or the C ₃ An apparatus for separating a majority of the components and a relatively less volatile fraction (44) containing a majority of the heavier hydrocarbon components,
  (1) dividing means for dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) a first heat exchange means (10) connected to the dividing means for receiving the first part (32) and sufficiently cooling it to partially concentrate (32a);
  (3) connected to the first heat exchange means (10) to receive the partially condensed first part (32a) into a vapor stream (34) and at least one liquid stream (35); Separating means (12 or 118e) for separating;
  (4) heat and mass transfer means (118d) connected to the dividing means and received in the processing assembly (118) for receiving and cooling the second part (33);
  (5) connected to the heat and mass transfer means (118d), accepts the cooled second portion (33a), further cools and substantially condenses (38a) a second Heat exchange means (10);
  (6) connected to the second heat exchange means (10) and accepts the substantially condensed second part (38a) and expands it to a lower pressure (38b) first expansion Means (14);
  (7) housed in the processing assembly (118) and connected to the first expansion means (14) to receive the inflated and cooled second part (38b) as a top feed thereto Absorption means (118c);
  (8) a second expansion means (15) connected to the separation means, receiving the steam stream (34) and expanding to the lower pressure (34a), further to the absorption means (118c); Second expansion means (15) connected to supply said expanded steam stream (34a) as a first bottom feed thereto;
  (9) a third expansion means (40a) connected to the separation means (12 or 118e) for receiving at least a portion (40) of the at least one liquid stream (35) and expanding to a lower pressure (40a); 17)
      (9a) further connected to said absorbing means (118c) to supply said expanded liquid stream (40a) as a second bottom feed thereto, or
      (9b) (i) the heat and mass transfer means (118d) has upper and lower regions;
            (Ii) connecting said processing assembly (118) to said third expansion means (17) to receive said expanded at least part of said at least one liquid stream (40a), said heat and mass transfer means; Leading between said upper and lower regions of (118d),
Third expansion means (17);
  (10) a steam collecting means (118b) housed in the processing assembly (118), connected to the absorbing means (118c) and receiving a distilled steam stream from an upper region of the absorbing means (118c);
  (11) further connected to the steam collecting means (118b) for receiving and heating the distilled steam stream (41), thereby supplying at least a portion of the cooling of the step (5), Heat exchange means (10);
  (12) further connected to the second heat exchange means (10) to receive and heat the heated distillation vapor stream, thereby supplying at least a portion of the cooling of the step (2). Followed by the first heat exchange means (10) for releasing the further heated distillation vapor stream (41a) as the volatile residual gas fraction (41d);
  (13) liquid collection means connected to the absorption means (118c) and contained in the processing assembly (118) for receiving a distilled liquid stream from a lower region of the absorption means (118c);
  (14) further connected to the liquid collecting means, receiving the distilled liquid stream, heating it and supplying at least part of the cooling in step (4), higher than coming out of the distilled liquid stream The heat that simultaneously strips volatile components and then releases the heated stripped distilled liquid stream from the processing assembly (118) as the relatively less volatile fraction (44). And mass transfer means (118d);
  (15) Adjusting the amount and temperature of the feed stream (38b, 39a, 40a) to the absorption means (118c) to recover most of the components in (44) in the relatively volatile fraction. Control means for maintaining the temperature of the upper region of the absorption means (118c) at such a temperature;
Equipped with the device.   Methane, C ₂ Ingredient C ₃ The gas stream (31) containing the components and the heavier hydrocarbon component, the volatile residual gas fraction (41d) and the C ₂ Most of the ingredients, said C ₃ Contains most of the components, and most of the heavier hydrocarbon components, or the C ₃ An apparatus for separating a majority of the components and a relatively less volatile fraction (44) containing a majority of the heavier hydrocarbon components,
  (1) dividing means for dividing the gas stream (31) into a first part (32) and a second part (33);
  (2) first heat exchange means (10) connected to the first dividing means for receiving and cooling the first part (32);
  (3) connected to the first heat exchange means (10) to receive the partially condensed first part (32a) into a vapor stream (34) and at least one liquid stream (35); Separating means (12 or 118e) for separating;
  (4) heat and mass transfer means (118d) connected to the dividing means and received in the processing assembly (118) for receiving and cooling the second part (33);
  (5) connected to the heat and mass transfer means (118d) and the separation means (12 or 118e), and at least one of the cooled second portion (33a) and the at least one liquid stream (35). A merging means for receiving the part (37) and forming a merged stream (38);
  (6) a second heat exchange means (10) connected to the merging means, receiving the merged stream (38), sufficiently cooling and substantially condensing it (38a);
  (7) connected to the second heat exchange means (10) and accepts the substantially condensed confluence stream (38a) and expands it to a lower pressure (38b) first expansion means ( 14)
  (8) Absorbing means housed in the processing assembly (118) and connected to the first expansion means (14) to receive the expanded and cooled combined stream (38b) as a top feed thereto (118c),
  (9) Second expansion means (15) connected to the separation means (12 or 118e), receiving the steam stream (34) and expanding to the lower pressure (34a), the absorption means A second expansion means (15) further connected to (118c) and supplying said expanded steam stream (34a) as a first bottom feed thereto;
  (10) Connect to the separation means (12 or 118e) to accept any remaining portion (40) of the at least one liquid stream (35) and expand to a lower pressure (40a) a third expansion Means (17),
        (10a) further connected to said absorbing means (118c) to supply said expanded liquid stream (40a) as a second bottom feed thereto, or
        (10b) (i) the heat and mass transfer means (118d) has upper and lower regions;
                (Ii) connecting the processing assembly (118) to the third expansion means (17) to receive any remaining expanded portion of the at least one liquid stream (40a); Leading between said upper and lower regions of moving means (118d),
Said third expansion means (17);
  (11) a steam collecting means (118b) housed in the processing assembly (118), connected to the absorbing means (118c) and receiving a distilled steam stream from an upper region of the absorbing means (118c);
  (12) further connected to the steam collecting means (118b) for receiving and heating the distilled steam stream (41), thereby providing at least a portion of the cooling of the step (6), Heat exchange means (10);
  (13) further connected to the second heat exchange means (10) to receive and heat the heated distillation vapor stream, thereby supplying at least a portion of the cooling of the step (2). Followed by the first heat exchange means (10) for releasing the further heated distillation vapor stream (41a) as the volatile residual gas fraction (41d);
  (14) liquid collection means connected to the absorption means (118c) and contained in the processing assembly (118) for receiving a distilled liquid stream from a lower region of the absorption means (118c);
  (15) further connected to the liquid collecting means, receiving the distilled liquid stream, heating it and supplying at least part of the cooling in step (4), higher than coming out of the distilled liquid stream The heat that simultaneously strips volatile components and then releases the heated stripped distilled liquid stream from the processing assembly (118) as the relatively less volatile fraction (44). And mass transfer means (118d);
  (16) Adjusting the amount and temperature of the feed stream (38b, 39a, 40a) to the absorption means (118c) to recover most of the components of (44) in the relatively volatile fraction. Control means for maintaining the temperature of the upper region of the absorption means (118c) at such a temperature;
Equipped with the device. 18. Apparatus according to claim 13 , 14 , 16 or 17 , wherein said separating means ( 118e ) is housed in said processing assembly ( 118 ) . (1) The gas collecting means ( 118e ) is accommodated in the processing assembly ( 118 ) ,
(2) Additional heat and mass transfer means are included within the gas collection means ( 118e ) , and the additional heat and mass transfer means include one or more paths leading to an external cooling medium. ,
(3) connecting the gas collecting means ( 118e ) to the merging means to receive the cooled gas stream ( 31a ) and further cool it by the external cooling medium and Lead to mass transfer means,
(4) said second dividing means, said gas contact with connection is allowed to collection means (118e), said further receiving the cooled gas stream (34), said first stream (36) and a second stream Divided into ( 39 ) ,
The apparatus according to claim 12 . (1) The gas collecting means ( 118e ) is accommodated in the processing assembly ( 118 ) ,
(2) Additional heat and mass transfer means are included within the gas collection means ( 118e ) , the additional heat and mass transfer means including one or more paths leading to an external cooling medium. ,
And (3) the gas collection means (118e) connected to said first heat exchange means (10), receives a first portion and said cooling (32a), further cooled by the external cooling medium To lead to said additional heat and mass transfer means,
(4) said second expansion means (15), said connection is allowed to the gas collection means (118e), said further receiving the cooled first portion (34), wherein from the inflated to a low pressure (34a ), Further connecting the second expansion means ( 15 ) to the absorption means ( 118c ) for supplying the expanded and further cooled first part ( 34a ) as the bottom feed thereto
The apparatus according to claim 15 . (1) Additional heat and mass transfer means are included within the separation means ( 12 or 118e) , and the additional heat and mass exchange means have one or more paths leading to an external cooling medium. Including
(2) directing the vapor stream to the additional heat and mass transfer means for cooling by the external cooling medium to form additional condensate;
(3) making the condensate part of the at least one liquid stream ( 35 ) separated therein;
The apparatus of claim 13 , 14 , 16 , 17 , or 18 . External heating in which the heat and mass transfer means ( 118d ) supplements the heating provided by the second part ( 33 ) to strip the higher volatile components exiting the distillation liquid stream. It includes one or more paths leading to the medium, according to claim 12, 13, apparatus according to 14,15,16,17,18,19,20 or 2 1,.

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