The method of separation of a gas stream and a device for its implementation (options)

 

(57) Abstract:

The hydrocarbon gas stream containing components1WITH2and C3share on volatile fraction comprising the major part WITH1and C2and heavier hydrocarbon components containing the major portion of the propane and propylene. The stream is cooled and/or expanded to partial condensation, then divided by the first flow of steam is directed into the contact device (absorber), where separating the third stream of vapor and liquid stream containing C3. The liquid stream containing C3, is sent to a distillation column where it is separated second stream of vapor containing a major part of the components of C3and heavier hydrocarbon components. Then the second steam flow is subjected to heat exchange with the third stream of steam for cooling the second stream of steam and condensation of at least part of it with the formation of the condensed stream. At least part of the condensed stream is sent to the contact device (absorber) for close contact with the first flow of steam. The remaining portion of the condensed stream is supplied to a distillation column as si is the column to maintain the temperature at the top of the contacting device and the distillation column at the level of the temperature, necessary to extract the main part of the final products. Device for separating gas containing embracing components1- C3and heavier hydrocarbons, includes one or more means for heat exchange and/or expanding gas to produce condensed gas stream, the distillation column to obtain a liquid stream containing a hydrocarbon, C3and steam flow, containing mainly WITH1and C2. The heat exchange means associated with the distillation column, which is also connected by a line of the first flow of steam in contact with the device, which receive the third stream of vapor and liquid stream containing C3. The control means is designed to regulate the quantities and temperatures in the contact device and the separating column. In the extract components C3more than 93% and provide full output components2in the residual gas stream. 6 C. and 4 h.p. f-crystals, 6 ill., 6 table.

The invention relates to a method of separating hydrocarbon containing gas.

Propane and heavier hydrocarbons can be extracted from various gases such as natural gas, free gas, and the synth is, is Ira oil, oil shale, bituminous Sandstone, and lignite. Natural gas typically consists mainly of methane and ethane, i.e., methane and ethane together constitute at least 50 mole percent of the gas. The gas also contains a relatively smaller number of heavier hydrocarbons such as propane, butane, pentane and the like, as well as hydrogen, nitrogen, carbon dioxide and other gases.

The present invention is mainly related with the extraction of propylene, propane and heavier hydrocarbons from such gas streams. It is desirable that the usual analysis of the gas stream, which will be processed in accordance with this invention, corresponded to approximately molar%, 92.6% methane, 4.7% ethane and other components of C2, 1.0% propane and other components of C3, 0.2% ISO-butane, 0.2% normal butane, plus 0.16% pentane, with balance restored with nitrogen and carbon dioxide. Gases containing sulfur, are also sometimes present.

Historical cyclical changes in the prices of natural gas, and an integral part of the liquefied natural gas (NGL) reduced the lucrative value of the propane and heavier components as liquid products. This caused the need for ways of materialov include such methods, based on the cooling and freezing of the gas absorption and oil absorption of the frozen oil. In addition, became popular cryogenic methods due to the availability of cheap hardware that creates energy during simultaneous expansion and heat from the gas, which is subjected to processing. Depending on the pressure of the source gas saturation (the content of ethane and heavier hydrocarbons) gas and the desired end products, can be used each of these methods.

Cryogenic method extension is now particularly preferred for the extraction of propane, because it provides maximum simplicity with easy start, control flexibility, high efficiency, safety, and reliability. U.S. patents NN 4157904, 4171964, 4251249, 4278457, 4519824, 4617039, 4687499, 4854955, 4869740, and 4889545, re-filed U.S. patent N 33408 together and applied N 08/337172 describe appropriate ways.

In conventional cryogenic method of extraction with extension of the original gas stream under pressure is cooled by heat exchange with other streams and/or due to external sources of freezing, such as compression-refrigeration is litely as fluids under high pressure, containing some of the desired components C3+. Depending on the saturation of gas and amount of liquids, which have been formed, a liquid with high pressure can be expanded and fractionated. The evaporation that occurs during the expansion of liquids, leads then to the cooling flow. Under certain conditions, pre-cooling of liquids with high pressure before expansion may be desirable to further decrease of temperature was the result of expansion. Advanced stream containing a mixture of liquid and vapor fractionized in distillation (deethanizer) column. In the column, enhanced cold flow(and) distilled(are) to separate residual methane, ethane, nitrogen, and other volatile gases at the top as a pair, from the desired components C3and heavier hydrocarbon components, located at the bottom as a liquid product.

If the source gas is not fully condensed (usually no), the vapor remaining from the partial condensate may be passed through the working expansion installation or engine, or the expansion valve to lower the pressure at which additional fluid conpre runs distillation column. Advanced stream then flows into the lower section of the absorption column and comes into contact with cold liquids for absorption components C3and heavier components from the vapor portion of the expanded stream. The liquid of the absorption column is then pumped into deethanizer column, in the upper intake to the column of raw materials.

The upper distillation stream from deethanizer comes into heat exchange with the residual gas from the absorption column and is cooled, condensing at least part of the distillation stream from deethanizer. The cooled distillation stream then flows into the upper section of the absorption column, where the cold liquid in the stream can come into contact with the steam part of an extended stream, as described previously. Usually, steam part (if any) cooled distillation stream and upper pairs of absorber are combined in the upper separation section in the absorption column as the residual methane and gaseous ethane product. Or chilled distillation stream can be fed to the separator for steam and liquid streams. Steam is combined with the contents of the upper part of absorbtion is="ptx2">

The separation that takes place in this way (producing residual gas obtained in this way, which contains substantially all of the components methane and C2in the source gas in the absence of mainly components of C3components and heavier hydrocarbons, and the fraction of sludge leaving deethanizer, which mainly contains all the components of C3components and heavier hydrocarbons in the absence of mainly methane, components C3or more volatile components), consumes energy for cooling the source gas, the evaporation deethanizer, irrigation deethanizer and/or re-compression of the residual gas. The present invention provides a means to achieve this separation, at the same time significantly reducing operational requirements (cooling, evaporation, irrigation, and/or re-compression) is needed to extract the desired products.

To achieve this, the technical result according to the present invention a method of separating a gas stream contains methane, the components of C2components C3and heavier hydrocarbon components, volatile residual gas fraction containing a major portion of the specified mamantov C3and heavier hydrocarbon components by processing the specified gas stream in one or more heat exchangers and/or expansion stages for the partial condensation of at least part of it and ensure that the at least first flow of steam and at least one liquid stream containing C3and lighter hydrocarbons, and direction, of at least one of these liquid streams containing C3in the distillation column for separation of the specified fluid to the second steam flow containing predominantly methane and components C2and indicated relatively less volatile fraction containing a major portion of these components C3and heavier hydrocarbon components, and the specified second vapour stream is cooled sufficiently to condense at least part of and education in the condensed stream, the part of the said condensed stream is served to the specified distillation column at a top feed position of the raw material, at least part of the said first steam flow is subjected to close contact, at least part of the remaining portion of the specified condensed stream and a liquid, containing C3specified fluid flow containing C3served in specified distillation column as a second raw for her, at least part of the said third stream of steam is directed to the heat exchange with the specified second steam flow and ensure that the cooling in the first stage and then unload at least some of the listed third of the steam flow in the form specified volatile fraction of residual gas, and the quantity and temperature of the flows of raw materials specified in the contact device and the specified distillation column are effective to maintain the upper temperature specified contact device and the specified distillation column at the level of the temperature, to get the main part of these components C3components and heavier hydrocarbons in the specified relatively less volatile fraction.

In addition, at least part of the said liquid stream containing C3is heated prior to its submission to the specified distillation column.

According to the present invention a device for the separation of gas contains methane, the components of C2components C3and banago methane and components C2and a relatively less volatile fraction containing a major portion of these components C3and heavier components containing one or more means for heat exchange and/or means for expanding, interconnected to provide at least one partially condensed gas stream and produce at least the first stream of steam and at least one liquid containing C3and lighter hydrocarbons, and a distillation column for receiving at least one of the liquid streams containing C3and to divide the specified stream to the second stream of steam containing predominantly methane and components C2and found relatively less volatile fraction containing a major portion of these components C3and heavier hydrocarbon components, and it includes a heat exchange associated with the specified distillation column, to obtain the second stream of steam and cool it sufficiently to condense at least part of and education in the condensed stream, separating means for receiving the above-mentioned condensed by giving into it specified the first fluid flow in the upper position of the feed, the contacting and separating means to receive at least part of the second fluid stream and at least part of the first steam flow and mixing at least one contacting device, such contacting and separating means includes a separating means for separating vapor and liquid after contact in the specified contact device to produce a third stream of vapor and liquid stream containing C3, and is associated with the specified distillation column to supply it to the specified fluid stream containing C3as the second source of raw materials and with the specified heat exchange direction, at least part of the third stream of steam for heat exchange with the specified second steam flow, and control means arranged to regulate the quantities and temperatures of the flows of raw materials specified in the contacting and separating means and the specified distillation column to maintain the upper temperature specified contacting and separating means and the distillation column at the level of temperature that can extract basically what="ptx2">

Additionally, the contacting and separating means connected with the second heat exchange, heating at least the part of the said liquid stream containing C3and linked to the distillation column to supply the specified heated fluid stream containing C3in specified distillation column as a second feedstock for her.

In accordance with the present invention, it was found that it is possible to support the extraction of C3more than 93%, at the same time providing a substantially complete removal of components C2in the residual gas stream. In addition, the present invention makes it possible, in the main, 100% separation of the components of C2and lighter components from components C3and heavier hydrocarbon components with low energy requirements. The present invention, although applicable at lower pressures and higher temperatures, is of particular advantage in the processing of the source gas in the pressure range from 400 to 800 psia (psia - pounds per inch squared), (28 to 56 kg/cm2or higher, under conditions requiring temperatures in the upper part of the column -50oF (-46oC) the payments. Reference drawings:

in Fig. 1 shows a diagram of the production process of the plant for the cryogenic natural gas processing corresponding to the previous level of technology;

in Fig. 2 shows a diagram of the production process of the plant for the cryogenic natural gas processing expansion corresponding to an alternative of the previous level of technology development, according to the re-filed U.S. patent N 33408;

in Fig. 3 shows a flow chart of a plant for the cryogenic natural gas processing expansion corresponding to an alternative of the previous level of technology development, according to the U.S. patent N 4617039;

in Fig. 4 shows a flow chart of the processing plant natural gas in accordance with the present invention;

in Fig. 5 shows a flow chart illustrating an alternative means for applying the present invention to a natural gas stream; and

in Fig. 6 shows a flow chart illustrating another alternative means of applying the present invention to a natural gas stream.

In the following explanation of the above figures, tables daunce text, values of flow velocities (in pound-moles per hour) rounded to the nearest integer values for convenience. The total flow rate shown in the tables include all non-hydrocarbonaceous components and, therefore, are mostly higher than the sum of the flow rates of the hydrocarbon components. The temperatures indicated are approximate values, rounded to the nearest value. It should also be noted that the calculations of the projected method, performed for comparison of the methods described in the figures and are based on the assumption that heat escapes from (or in) the environment in (or from) the process scheme. The quality of commercially available insulating materials makes this is a very important assumption, which is usually done by specialists in this field.

The previous level of technology

According Fig. 1, the reproducing method of the previous level of technology, the feed gas enters the plant as stream 31 at a temperature of 80oF (27oC) and a pressure of 580 psia (40.8 kg/cm2). If the feed gas contains a concentration of sulfur compounds, which may impede the flow of product to meet the technical at the th, the flow of raw materials usually dehydratases to prevent the manifestation of hydration (ice) in cryogenic conditions. Usually for this purpose, applied solid desiccant.

The original stream is cooled to -97oF (-71oC) (thread 31A) in exchanger 10 by heat exchange with cool residue gas at -108oF (-78oC) (stream 34) and liquid separator/absorber when -108oF (-78oC) (stream 35A). (The decision whether to use more than one heat exchanger for the specified work on the cooling will depend on a number of factors, including but not limited to, the flow velocity of the incoming gas, the size of the heat exchanger, temperature, flow etc)

In a previous application of this method, corresponding to the previous level of technology, the cooled flow of raw materials 31A consistently distillable under pressure, while the flow of the feedstock was suitable at a lower pressure than in this example. Specialists in this field will be recognized that this thread is impossible to distil effectively when the pressure of the source gas used in this example. Accordingly, the cooled feed stream of raw materials is the first instant the advanced thread the pressure (approximately 470 psia (33 kg/cm2)) dividing absorption tower 15. During expansion, the effect of Joule-Thomson, also cools the flow of the feedstock. In the method illustrated in Fig. 1, the expanded stream 31b, leaving the expansion valve 13, is exposed to high temperature -108oF (-78oC) and is served in the absorbent section 15b in the lower zone of the separator/absorber tower 15. The liquid portion of the expanded stream is mixed with the liquid flowing downward from the absorbing section 15b, and the combined stream 35 leaves the bottom of separator/absorber 15. The steam portion of the expanded stream rises upward through the absorbing section 15b and exposed to a cold fluid flowing down.

The separator/absorber tower 15 is a conventional distillation column consisting of a set of vertically mounted chutes, one or more layers of the nozzle, or some combination of gutters and spouts. As it often takes place at the processing plants natural gas, the separator/absorber tower can consist of two sections. The upper section 15a is a separator where any pairs located in the upper part of the raw material is separated from the liquid part, and where poomse available) above the raw material for the formation of cold distillation stream 42, which leaves the upper part of the tower. Located below the absorbent section 15b includes a groove and/or the nozzle and provides the necessary contact between the liquids falling downward and the vapors rising upward for condensation and absorption of propane and heavier components.

The combined liquid stream 35 leaves the bottom part of the separator/absorber 15 at -108oF - 78oC). He served as the feedstock middle part of the column (stream 35b) deethanizer 17 pump 16 after he will provide cooling of the source gas in the exchanger 10, as described earlier. Deethanizer in tower 17, working under pressure 480 psia (34 kg/cm2), is also a conventional distillation column containing many vertically installed gutters, one or more layers of the nozzle, or some combination of gutters and spouts. Deethanizer tower may also consist of two sections: the upper section 17a, where any vapor contained in the upper part of the raw material is separated from the liquid part, and where the steam rising from the lower distillation or deethanizing section 17b, combined with Park 36, which leaves the upper part of the tower; and the lower, deethanizing section 17b, which contains a groove and/or the nozzle in order to provide the necessary contact between the liquids falling downward and the vapors rising upward. Deethanizer section 17b also includes the evaporator 18, which heats and vaporizes the liquid at the bottom of the column to provide eye vapors that rise to the top of the column to drive the liquid product stream 37, methane and components C2. Usually the bottom liquid product is characterized by the fact that it contains ethane and propane in a ratio of 0.02:1 to mullarney basis. The flow of liquid product 37 leaves the lower part of the column at a temperature of 215oF (102oC) and is cooled to a temperature of 110oF (43oC) (stream 37A) in the heat exchanger 19 before entering the store.

Above the steam flow 36 leaves deethanizer tower 17 -19oF - 28oC) and partially condensed by heat exchangers 24 and 25 by using a propane refrigerant temperature -40oF (-40oC) and ethane refrigerant with a temperature of -85oF (-65oC), respectively. The partially condensed stream 36b, now at a temperature of -80oF (-62oC) and pressure Noah fluid. The pump 27 is used to supply part of the condensed liquid (stream 41) in the upper part deethanizer tower 17 as irrigation. The remaining portion of the condensed liquid (stream 40) is fed by a pump 27 in the upper part of separator/absorber 15 as a cold liquid, which in contact with the steam rising up through the absorbent section 15b, as described earlier.

Drum for irrigation 26 is introduced into the work, in General, when the same pressure as the separator/absorber 15, i.e. at a pressure of about 10 psia (0.7 kg/cm2below the operating pressure of deethanizer 17. This allows steam (stream 38) is partially condensed matter content of the upper part of deethanizer (stream 36b) to unite with the cold distillation stream 42 from the upper part of separator/absorber 15 to education stream 34 cold residual gas. The residual gas stream passes in the reverse direction to the flowing of the source gas in heat exchanger 10 where it is heated to 48oF (9oC) (stream 34a). The residual gas is then used for cooling the propane refrigerant under high pressure in the heat exchanger 28 to heat the residual gas to the 70oF (21oC) (thread 34b) prizhivaniya due to compression of the residual gas, but the result is, in General, the total reduction in power consumption.) The compressor 22 is driven by using an additional source of energy for compression of the residual gas (stream 34) to the value of the line pressure consumption (usually in the range of inlet pressure). After cooling in unloading the refrigerator 23, residual gas product (stream 34d) is sent to the gas consumer at a temperature of 110oF (43oC) and pressure 613 psia (43 kg/cm2).

Summary regarding flow rates and energy consumption in the manner illustrated in Fig. 1, is presented in table. I.

In the example of the previous level of technology, which is illustrated in Fig. 1, the residual gas (stream 34) consists of gas, located in the upper part of separator/absorber (stream 42), and steam (stream 38) remaining after the partial condensation product in the upper part of deethanizer (stream 36). Essentially, the product is at the top of deethanizer should be cooled to a sufficiently low temperature -80oF (-62oC) so, basically, the entire propane, which it contains, condensed, and did not stand out in the stream 38, and so that a portion (stream 40) end of the condensed liquid, which is open, which is contained in the steam part of the cooled expanded stream 31b raw material when it is exposed to in the absorbent section 15b. Since there is no flow method, suitable at appropriate temperatures, to provide the cooling needed for the partial condensation product of the upper part of deethanizer, for this purpose should be used external mechanical refrigerator (evaporation of the propane refrigerant in the heat exchanger 24 and ethane refrigerant in the heat exchanger 25), adds a significant amount of energy consumed to compress when frozen.

One of the ways to achieve extraction of the desired propane while reducing energy consumption is changing the way by which to produce a cold liquid supplied to the upper part of the separator/absorber, so that the cooling load could better match the temperature levels suitable flow method. Fig. 2 represents an alternative way of previous level of technology in accordance with the re-filed U.S. patent N 33408 that achieves this goal. The method of Fig. 2 was applied to the same part of the source gas and the same conditions as to describe the existing conditions with the in order to minimize energy costs for a given level of extraction of propane.

Thread 31 of the feedstock is cooled in exchanger 10 by heat exchange with cool residue gas at a temperature of -104oF (-76oC) (stream 34a) and the cold source liquids (stream 47A) deethanizer at a temperature of -58oF (-50oC). The cooled stream 31A enters separator 11 at a temperature of -81oF (63oC) and a pressure of 570 psia (40 kg/cm2), where the vapor (stream 32) is separated from the condensed liquid (stream 33).

Vapor (stream 32) of the separator 11 is included in the working expansion installation 13, in which mechanical energy is released from this part of the feedstock with high pressure. Installation 13 extends pairs, mainly isoentropic from pressure of about 570 psia (40 kg/cm2) to a pressure of about 425 psia (30 kg/cm2) (operating pressure of separator/absorber), with the work expansion cooling the expanded stream 32A to a temperature of approximately -104oF (-76oC). Conventional commercially available expanders are capable of removing about 80-85% of production is theoretically available in an ideal isoentropic expansion. Products which happens often used ctober compression of the residual gas stream 34b).

The expanded and partially condensed stream 32A included in the upper section of the intermediate separator 29. Liquid (stream 33) in the separator extends similarly to a pressure of 425 psia (30 kg/cm2with the help of the expansion valve 12, cooling stream 33 to -95oF (-70oC) (stream 33a) before it enters the bottom section of the intermediate separator 29. Part of the flow 33a, which evaporates during the immediate expansion (stream 45), leaving the bottom section of the intermediate separator 29 and enters the upper section for connection with a steam part of the expanded stream 32A, forming the combined steam flow 43, which then enters the separator/absorber 15. Part a pair 32A, which condenses during expansion (stream 44), leaving the upper section of the intermediate separator 29 and enters the bottom section to connect with the liquid part instantly extended thread 33a, forming a combined stream 46 of the liquid, which then flows to the pump 30.

The combined stream 43 steam enters the lower section of separator/absorber 15 at a temperature of -104oF (-76oC) and a pressure of 425 psia (30 kg/cm2). While the steam rises through the tower, he is exposed to a cold fluid, steichele/absorber 15 (stream 35) is pumped by pump 16 (stream 35A) for connection with the combined stream 46a fluid, leaving the pump 30, forming the original thread 47 for deethanizer. Stream 47 is heated from -100oF (-73oC) -58 tooF (-50oC) (thread 47A) at that time, as it provides cooling in the heat exchanger 20, and from -58oF (-50oC) to 65oF (18oC) (thread 47b) at that time, as it provides cooling in the heat exchanger 10. Stream 47b then served in deethanizer 17 (operating at a pressure of 490 psia (34 kg/cm2)) as a feedstock middle part of the column will be Athanasia methane and components C2. Thread 37 of the liquid product leaving the bottom part of deethanizer at a temperature of 218oF (103oC) and is cooled to a temperature of 110oF (43oC) (stream 37a) in the heat exchanger 19 to the directions in the repository.

Above the stream 36 a pair of leaves deethanizer tower 17 at a temperature of 15oF (-9oC) and partially condensed by heat exchanger 24 through the use of propane refrigerant at a temperature of -40oF (-40oC). The partially condensed stream 36A, now at a temperature of -35oF (-37oC) and a pressure of 485 psia (34 kg/cm2), is the drum 26 for irrigation and is divided into stream pair 38 and the thread 39 of the condensed liquid. The pump 27 is used to podcast part of the condensed liquid (stream 40), leaving the pump 27, is connected with the thread 38 for education combined stream 42.

The combined stream 42 enters, via a heat exchanger 20, heat exchange with the stream 34 of the pair of the upper part of the separator/absorber, and flow 47 feedstock of deethanizer, resulting in cooling and substantial condensation of stream. Substantially condensed stream 42A at a temperature of 110oF (-79oC) then instantly expanded using the appropriate expansion device, such as expansion valve 28, to the operating pressure (approximately 425 psia (30 kg/cm2)) separator/absorber tower 15. The drum 26 for irrigation is driven mainly at a pressure exceeding the operating pressure of separator/absorber 15 (about 60 psia (4 kg/cm2)). As a result, the portion of the stream 42A evaporates during expansion, providing further cooling of the total stream. In the method, which is illustrated in Fig. 2, the expanded stream 42b extending from the expansion valve 28 reaches temperature - 113oF (-80oC) and then fed to the separation section of the separator/absorber tower 15 as the cold liquid that comes in contact with the item is part of separator/absorber 15 at a temperature -111oF (-79oC) is a flow 34 cold residual gas. The residual gas stream passes in the opposite direction to the combined stream 42 in the heat exchanger 20 and is heated to a temperature of -104oF (-76oC) (stream 34a), while it provides cooling and substantial condensation of the combined stream. The residual gas is further heated to 54oF (12oC) (thread 34b) while he goes in the opposite direction to the flowing of the source gas in the heat exchanger 10. The residual gas is then re-compressed in two stages. The first stage is carried out by the compressor 14 driven expansion installation 13. The second stage is compressor 22 driven by an additional energy source, which compresses the residual gas stream 34d) to line pressure consumption. After cooling in unloading the refrigerator 23, residual gas product (stream a) is included in the pipeline of the consumer at a temperature of 110oF (43oC) and pressure 613 psia (43 kg/cm2).

Summary regarding flow rates and energy consumption in the method illustrated in Fig. 2, is presented in table. II.

Comparison of energy consumption in the table. II, ol the persons of Fig. 2 carries mainly at reducing compression by freezing and load evaporator deethanizer compared with those of the method of Fig. 1 for a given level of extraction of propane. This is achieved by application of the method flow for cooling, which is required for cold flow as a feedstock in the upper part of separator/absorber tower 15. The method of Fig. 2 still requires the use of external mechanical freezing (evaporation of the propane refrigerant in the heat exchanger 24) for the partial condensation of the contents of the upper part of deethanizer (stream 36). Essentially, the design of the plant, which is based on the method of Fig. 2, must have capital costs associated with the introduction of compression-refrigeration system propane.

Fig. 3 represents an alternative method of the previous level of technological development in accordance with U.S. patent N 4617039 that achieves retrieve the desired propane, using a simpler, less expensive factory fixture. The method of Fig. 3 is based on the same composition of the source gas and the same conditions as described above in Fig. 1 and 2. When implementing this method, the flow source is/SUP>F (-71oC) (stream 34a) and liquids from the separator at a temperature of -91oF (-68oC) (stream 33a). The cooled stream 31A enters separator 11 at a temperature of -73oF (-58oC) and a pressure of 570 psia (40 kg/cm2), where the vapor (stream 32) is separated from the condensed liquid (stream 33).

Vapor (stream 32) of the separator 11 is included in the working expansion installation 13, in which mechanical energy is extracted from this portion of the feedstock with high pressure. Installation 13 extends pairs, mainly isoentropic from pressure of about 570 psia (40 kg/cm2) to a pressure of about 353 psia (25 kg/cm2) (operating pressure of separator/absorber 15), with the work expansion cooling the expanded stream 32A to a temperature of approximately -110oF (-79oC). The expanded and partially condensed stream 32A included in the lower section of separator/absorber 15. The liquid portion of the expanded stream is mixed with the liquid flowing down from the adsorption section, and the combined liquid stream 35 leaves the lower part of separator/absorber 15 at a temperature -111oF (-79oC). The steam portion of the expanded stream rises upward through the absorbing section and exposed to a cold fluid, STK 35 of the liquid from the bottom of separator/absorber 15 is served as a cold source of raw materials (stream 35A) the upper part of the column in deethanizer 17 by the pump 16. Liquid (stream 33) delimiter instantly expanded to a pressure slightly exceeding 368 psia (25.9 kg/cm2) operating pressure deethanizer 17 through which extends the valve 12, cooling stream 33 to a temperature of -91oF (-68oC) (stream 33a) before it will provide cooling of the incoming source gas as described previously. Stream 33b, now at a temperature of 650oF (18oC), then flows into deethanizer 17, in the place of receipt of raw materials in the middle part of the column, in order from him were distilled methane and components C2. Thread 37 of the liquid product leaving the bottom part of deethanizer at a temperature of 186oF (86oC) and cooled to 110oF (43oC) (stream 37A) in the heat exchanger 19 before he was sent to the vault.

The effective pressure in deethanizer 17 is maintained slightly higher than the operating pressure of separator/absorber 15. This allows the pair (stream 36) in the upper part of deethanizer to push the flow through the heat exchanger 20 and thence into the upper section of separator/absorber 15. In the heat exchanger 20, the contents of the upper part of deethanizer at a temperature of -210oF (-29oC) is in heat exchange with the contents (stream 34) the upper part of the separator and the cell stream is then served in the separation section of the separator/absorber tower 15, so its condensed liquid is separated in order to become a cold liquid, which in contact with the vapors rising upward through the absorbing section.

Distillation stream leaving the upper part of separator/absorber 15 at a temperature -117oF (-83oC) is a flow 34 cold residual gas. The residual gas stream passes in the opposite direction to located in the upper part of deethanizer stream 36 in the heat exchanger 20 and is heated to -97oF (-71oC) (stream 34a) at that time, as it provides cooling and partial condensation of the stream in the upper part of deethanizer. The residual gas is heated further up to 75oF (24oC) (thread 34b) while he goes in the opposite direction to the flowing of the source gas in the heat exchanger 10. The residual gas is then re-compressed in two stages. The first stage is carried out by the compressor 14 driven expansion installation 13. The second stage is compressor 22 driven by an additional energy source, which compresses the residual gas stream 34d) to line pressure consumption. After cooling in unloading the refrigerator 23, residual gas product (at the P>).

Summary regarding flow rates and energy consumption for the method illustrated in Fig. 3, is presented in table. III.

Comparison of energy consumption in the table. III provided for the method of Fig. 3, with energy consumption in the table. II, corresponding to the method of Fig. 2 shows that the method of Fig. 3 reaches the desired level of extraction of propane at approximately the same total compression load and the load of the evaporator deethanizer, as in the method of Fig. 2. The decision whether to use a simpler, less expensive method of Fig. 3, instead of the method of Fig. 2, will often depend on such factors as the relative cost of heat and power compression, size of plant, etc. it Should be noted, incidentally, that the success of the method of Fig. 3 depends on absorption cooling effect, which occurs inside the separator/absorber 15, where the saturated vapour rising up through the tower by evaporation of liquid methane and ethane, contained in the stream 36A, provide freeze in the tower. Note, the result is that as steam, leaving the upper part of the tower, and the liquid leaving the bottom of the tower, are colder than the corresponding flows of raw materials in these concat cooling, required in the heat exchanger 20 to the partial condensation of the contents of the upper part of deethanizer (stream 36) without having to deethanizer 17 worked at a pressure substantially higher than the pressure of separator/absorber 15. It was otherwise with the method of Fig. 2, where it was necessary cooling method Joule-Thomson condensed stream in the upper part of deethanizer in order to provide the driving force temperature, which made possible the appearance of the heat exchange.

Description of the invention

Example 1. Fig. 4 illustrates the scheme of the manufacturing process in accordance with the present invention. The composition of the source gas and the conditions that are considered in the method shown in Fig. 4 are the same as in Fig. 1-3. Accordingly, the method of Fig. 4 can be compared with the methods of Fig. 1-3 to illustrate the advantages of the present invention.

Currently playing in Fig. 4 method, the source gas is supplied at a temperature of 80oF (27oC) and a pressure of 580 psia (40.8 kg/cm2) as stream 31. Thread 31 of the feedstock is cooled in exchanger 10 by heat exchange with cool residue gas at a temperature of -88oF (-67oC) (stream 34a), with the liquids from the separator when those whooC) (stream 35A). The cooled stream 31A enters separator 11 at a temperature of -78oF (-61oC) and a pressure of 570 psia (40 kg/cm2), where the vapor (stream 32) is separated from the condensed liquid (stream 33).

Vapor (stream 32) of the separator 11 is included in the working expansion installation 13, in which mechanical energy is extracted from this portion of the feedstock with high pressure. Installation 13 extends pairs, mainly isoentropic from pressure of about 570 psia (40 kg/cm2) to a pressure of about 396 psia (28 kg/cm2) (operating pressure of separator/absorber 15), with the work expansion cooling the expanded stream 32A to a temperature of approximately -107oF (-77oC). The expanded and partially condensed stream 32A included in the lower section of separator/absorber 15. The liquid portion of the expanded stream is mixed with the liquid flowing down from the adsorption section, and the combined liquid stream 35 leaves the lower part of separator/absorber 15 at a temperature -108oF (-78oC). The steam portion of the expanded stream rises upward through the absorbing section and exposed to the cold liquid falling downward to condense and absorption of propane and heavier components.The effective pressure in deethanizer 17 is supported somewhat above codeprivate flow through the heat exchanger 20 and thence into the upper section of separator/absorber 15. In the heat exchanger 20 the contents of the upper part of deethanizer at a temperature of -25oF (-32oC) is in heat exchange with the contents of the upper part (stream 34) of separator/absorber 15, the cooling flow to -112oF (-80oC) (stream 36A) and partially condensing it. The partially condensed stream is then served in the separation section of the separator/absorber tower 15, where the condensed liquid is separated from unfused pair. Unfused pairs is combined with the steam rising from the lower absorbent section for the formation of cold distillation stream 34, leaving an upper zone of separator/absorber 15. The condensed liquid is separated into two parts. One portion, stream 40, is directed at the bottom absorbent section of separator/absorber 15 as a cold liquid, which comes into contact with the vapors rising upward through the absorbing section. The other part, the thread 39, served in deethanizer 17 as irrigation pump 21, with irrigating stream 39A fed into the top spot of the receipt of raw materials in deethanizer 17 at a temperature of -112oF(-80oC).

Distillation stream leaving the upper part of separator/absorber 15 prohodit in the opposite direction to located in the upper part of deethanizer stream 36 in the heat exchanger 20 and is heated to -88oF (-67oC) (stream 34a) at that time, as it provides cooling and partial condensation of the stream in the upper part of deethanizer. The residual gas is heated further up to 75oF (24oC) (thread 34b) at that time, as he passes in the reverse direction to the flowing of the source gas in the heat exchanger 10. The residual gas is then re-compressed in two stages. The first stage is carried out by the compressor 14 driven expansion installation 13. The second stage is compressor 22 driven by an additional energy source, which compresses the residual gas stream 34d) to line pressure consumption. After cooling in unloading the refrigerator 23, residual gas product (stream a) is included in the pipeline of the consumer at a temperature of 110oF (43oC) and pressure 613 psia (43 kg/cm2).

Summary regarding flow rates and energy consumption for the method illustrated in Fig. 4, is presented in table. IV.

Comparison of energy consumption in ways corresponding to the previous level of technology, which are shown in the table. I, II, and III, energy use in the present invention, which is shown in the table. IV, shows that the present efficiency of the compression and the need to use heat. Power compression by more than twelve percent lower than in any of the methods corresponding to the previous level of technology, while the need to use heat more than twenty-seven percent lower than in any of the methods corresponding to the previous level of technology.

Comparing the present invention with a method corresponding to the previous level of technology shown in Fig. 3, note the temperature of the fluid separator/absorber (stream 35A in Fig. 3 and the flow 35b in Fig. 4) in the place of receipt of raw materials in deethanizer 17. In the method of Fig. 3, these fluids are served in deethanizer as cold feedstock top. However, the temperature of the steam in the upper part of deethanizer -21oF (-29oC), much higher than the temperature of -110oF (-79oC) the original thread 35A, indicating that the raw materials of the upper part is much colder than necessary to maintain the desired propane and concentration of the heavier component in the upper part of the tower. In the method of Fig. 4, the flow of raw materials (stream 35b) is deethanizer when -46oF (-43oC) at the lower position of the point of entrance of the feedstock. This is much closer to the temperature of the second raw material, needed to achieve the desired content of propane and heavier component in the product of the upper part of the installation. As a result, requires only a small flow irrigation, stream 39A, to the top of deethanizer 17 intended for the receipt of raw materials, with the method of Fig. 4. Significantly lower load on the evaporator when the method of Fig. 4 is a further indication of the best match between the temperature of the feedstock of the tower and flows of the desired product of the tower.

By fluid feed separator/absorber in deethanizer Fig. 4 if more than the optimum temperature, increases not only the performance of deethanizer (as a reflection of a lower load on the evaporator), the ability to freeze these fluids can be implemented at a lower temperature level, which allows for part load cooling process. These fluids, which help cool the incoming source gas in heat exchanger 10, the cooling of the residual gas (stream 34a) must ensure that the heat exchanger 10, is reduced. As a result, the residual gas may enter the heat exchanger 10 at a higher temperature, which, in its Cherednychenko, residual gas enters the compressor 14 at a higher pressure in the method of Fig. 4 and, therefore, require lower power compression to bring the residual gas pressure in the pipeline.

Example 2. Fig. 4 represents a preferred variant of the present invention under the conditions of temperature and pressure are shown, because it usually provides the most simple factory equipment for a given level of extraction component C3. A somewhat more complex structure, which supports the same extraction component C3basically, with the same energy consumption, can be achieved by the application of another embodiment of the present invention, as illustrated in the method of Fig. 5. The composition and conditions of the source gas, is considered in the manner that shown in Fig. 5 are the same as in Fig. 1-4. Accordingly, the method of Fig. 5 can be compared with the methods of Fig. 1-3 to illustrate the advantages of the present invention, and similarly can be compared to the variant shown in Fig. 4.

Currently playing in Fig. 5-way, cooling and expansion of the source gas is basically the same as the scheme used is the upper part of deethanizer 17. According Fig. 5, the thread 36 at the 8oF (-13oC) included in the heat exchanger 24 and enters into the heat exchange with the partially heated combined stream (stream 35b) fluid, which is pumped from the separator/absorber tower 15, the cooling stream 36 and partially condensing it. The partially condensed stream 36A enters the drum 26 for irrigation at a temperature of -22oF (-30oC) and pressure 410 psia (28,1 kg/cm2), where the unfused pairs (stream 38) is separated from the condensed liquid (stream 39). The condensed liquid returns to deethanizer 17 as irrigation (flow 39A) via a pump 27 for irrigation, getting in deethanizer at a temperature of -22oF (-30oC) in the upper source of the feedstock. Further, the heated stream (stream 35C) of the joint fluid, which leaves the heat exchanger 24, enters deethanizer 17 at a temperature of 2oF (-17oC) the place of supply of raw materials in the middle part of the column. In deethanizer, threads 35C and 33b (coming in a relatively downstream location of the supply of raw materials in the middle part of the column) are the distillation of methane and components C2. The resulting stream 37 liquid product leaves the bottom part of deethanizer when templenet in the store.

The effective pressure drum 26 for irrigation is supported slightly above the current pressure of separator/absorber 15. This allows unfused couple (stream 38) to push the flow through the heat exchanger 20 and then into the upper section of separator/absorber 15. In the heat exchanger 20, the flow of steam at a temperature of -22oF (-30oC) enters into a heat exchange with the contents of the upper part (stream 34) of separator/absorber 15, the cooling flow to -112oF (-80oC) (stream 38A) and partially condensing it. The partially condensed stream is then served in the separation section of the separator/absorber tower 15 so that the condensed part was separated to become cold liquid, which in contact with the steam rising up through the absorbent section.

Distillation stream leaving the upper part of separator/absorber 15 at a temperature -113oF (-81oC) is a flow 34 cold residual gas. The residual gas stream passes in the opposite direction to the flow 38 of the steam in the heat exchanger 20 and is heated to -88oF (-67oC) (stream 34a) at that time, as it provides cooling and partial condensation of the stream. The residual gas is heated further on the memory in the heat exchanger 10. The residual gas is then re-compressed in two stages. The first stage is carried out by the compressor 14 driven expansion installation 13. The second stage is compressor 22 driven by an additional energy source, which compresses the residual gas stream 34d) to line pressure consumption. After cooling in unloading the refrigerator 23, residual gas product (stream a) is included in the pipeline of the consumer at a temperature of 110oF(43oC) and pressure 613 psia (43 kg/cm2).

Summary regarding flow rates and energy consumption for the method illustrated in Fig. 4, is presented in table. V.

Comparison of energy consumption is presented in table. I, II and III for methods Fig. 1, 2 and 3 with the data given in table. V for the method of Fig. 5 shows that this variant of the present invention also reduces the energy consumption for a given level of extraction component C3compared with the method of the previous technology. Power compression by more than twelve percent lower than in any of the methods of the previous level of technology, while the need to use heat more than twenty-eight p is zestawienie in table. IV and V for the methods of Fig. 4 and 5, shows that a variant of the present invention in Fig. 5 requires a little more power compression (about 0.25 percent) than Fig. 4, but uses about 1.7 percent less consumption of heat for the evaporator deethanizer. These two variants of the present invention are basically the same General standard requirements. The choice of whether to include additional equipment required by the method of Fig. 5, will depend primarily on factors that include the size of the plant and the availability of equipment, as well as comparative cost of power compression and heat use.

Example 3. The third variant of the present invention shown in Fig. 6, which uses a simpler version of the present invention. The composition of the initial gas conditions, rassmatrivaemye in ways that are illustrated in Fig. 6 are the same as in Fig. 1-5.

Currently playing in Fig. 6-way, cooling and expansion of the source gas is basically the same as the scheme used in the method of Fig. 4. The difference lies in the location of the combined flow of the liquid from separator/absorber 15 after it is partially heated (stream 35b) by ooF (-80oC) to -45oF (-43oC) in the heat exchanger 10, as it provides cooling of the incoming source gas, as described previously in example 1. The heated stream, the stream 35b, then served in deethanizer 17 in the top spot entering the column of raw materials, where after entering the tower at a temperature of -45oF (-43oC) from it distills the methane and components C2. Received, as a result, the flow of 37 liquid product exits the bottom of deethanizer at a temperature of 191oF (88oC) and cooled to 110oF (43oC) (stream 37A) in the heat exchanger 19 before entering the store.

The effective pressure in deethanizer 17 is supported slightly above the current pressure of separator/absorber 15. This allows the pair (stream 36) in the upper part of deethanizer to push the flow through the heat exchanger 20 and thence into the upper section of separator/absorber 15. In the heat exchanger 20 the contents of the upper part of deethanizer at a temperature of -15oF (-26oC) enters into a heat exchange with the contents of the upper part (stream 34) of separator/absorber 15, the cooling flow to -114oF (-81oC) (stream 36A) and partially condensing it. The partially condensed stream is served at the lalas, becoming cold liquid, which in contact with the steam rising up through the absorbent section.

Distillation stream leaving the upper part of separator/absorber 15 at a temperature of -115oF (-82oC) is a flow 34 cold residual gas. The residual gas stream passes in the opposite direction to the thread 36 of the upper part of deethanizer in the heat exchanger 20 and is heated to -71oF (-57oC) (stream 34a), while it provides cooling and partial condensation of the stream top of deethanizer. The residual gas is heated further up to 75oF (24oC) (thread 34b), while he goes in the opposite direction to the flowing of the source gas in the heat exchanger 10. The residual gas is then re-compressed in two stages. The first stage is carried out by the compressor 14 driven expansion installation 13. The second stage is compressor 22 driven by an additional energy source, which compresses the residual gas stream 34d) to line pressure consumption. After cooling in unloading the refrigerator 23 residual gas product (stream a) is included in the pipeline of the consumer at a temperature of 110oF (43oC) both, illustrated on Fig. 6, is presented in table. VI.

Comparison of energy consumption is presented in table. I, II and III for methods Fig. 1, 2 and 3 with the data given in table. VI for the method of Fig. 6 shows that this variant of the present invention uses less total energy for a given level of extraction component C3than the methods of the previous technology. Power compression is basically the same (about 0.5%) as the lowest value that can be used in any method according to the preceding level of technology, at the same time need to be used to heat more than nine percent lower than in any method according to the previous technology. Thanks a simpler device than in the embodiments of Fig. 4 and 5, a variant of the Fig. 6 of the present invention can provide advantages for capital costs that outweigh its higher energy consumption compared with other options. The choice between the variants of Fig. 4, 5 and 6 of the present invention will often depend on factors such as plant size, availability of equipment, and the economic balance of capital expenditure compared to operating costs.

As described previously, in the preferred embodiment, located in the upper part of the pair is partially condensed and used for absorption of valuable components C3and heavier components from the vapors leaving the working expansion installation. However, the present invention is not limited to this option. It may be advantageous, for example, to process only one portion facing the pair of expansion of the working setup this way, or to use only a portion located in the upper part of the condensate as an absorbent, in cases where other constructive consideration shows that part of the product emerging from the expansion of the installation, or condensate, located in the upper part, can do without the separator/absorber. Conditions of the source gas, the size of the plant, availability of equipment, or other factors may indicate the abolition of the expansion in the working installation 13, or replacement of the alternate expansion device (such as an expansion valve), is possible, or what the total (rather than partial) condensation of the upper flow is possible or preferable in the heat exchanger 20. It should also be noted that the separator/absorbe is the use of the present invention, it is necessary to have a small difference in pressure between deethanizer and separator/absorber, which must be taken into account. If located in the upper part of the pair pass through the heat exchanger 20 in the separator/absorber 15 without any increase of pressure in the separator/absorber must have a working pressure slightly below the operating pressure of deethanizer 17. In this case, the combined stream of liquid flowing from separator/absorber can be pumped into the place of supply of raw materials in deethanizer. The alternative is the provision of an auxiliary fan on the steam pipeline in order to raise the working pressure in the heat exchanger 20 and the separator/absorber 15 and of sufficient magnitude so that the combined stream of liquid may be made (after heat exchange with other streams of way as described in examples 1, 2 and 3) in deethanizer 17 without using the pump. Yet another alternative is to install the separator/absorber at sufficient height with respect to the place of supply of raw materials on deethanizer 17 so that the hydrostatic pressure of the liquid is compensated for the pressure difference.

Use and distribution of liquids separator and liquids the underwater gas, and the stream selection method for servicing a specific heat exchange must be evaluated for each specific application. In addition, there might be an external freezing to Supplement the cooling available to the source gas from the other threads of the process, in particular, in the case of gas, more saturated than the one that was used in example 1.

It should also be recognized that the relative amount of raw materials found in each branch of the condensed liquid contained in the stream 36A, which is divided between the two towers of Fig. 4, will depend on several factors, including gas pressure, the composition of the source gas and the value of available capacity. Optimum separation is usually impossible to predict without assessing the particular circumstances of the specific application of the present invention. The provisions of the places of receipt of raw materials in the middle part of the column shown in Fig. 4-6, are the preferred positions for carrying out the method described. However, the relative location of the places of receipt of raw materials in the middle part of the column may vary depending on the composition of supply of raw materials or other is whether parts of it, can be combined depending on the relative temperature and the quantities of individual threads, and the combined stream is supplied then in the place of receipt of raw materials in the middle part of the column. Fig. 4-6 are better options in the compositions of the products and the conditions of pressure are shown. Although the extension is a separate thread was made in the data expansion devices can be used an alternative expansion funds where appropriate. For example, conditions may warrant work expansion of the stream (stream 33) of the condensed liquid.

The present invention provides an improved extraction of the components of C3by the amount of energy used, which is required for carrying out the method. Improvements in energy use, which is required for the action method using deethanizer may be in the form of reduction needs power for compression or re-compression, reducing the need power for external freezing, reducing energy needs for tower evaporators, or combinations thereof. On the contrary, if it is desirable, enhanced recovery component C3you can get it if fixirovannomu of the invention, experts in this field agree that it can be carried out also other and further modifications, for example, to adapt the invention to various conditions, types of raw materials or other requirements without removal from the essence of the present invention, as defined by the following claims.

1. Method of separating a gas stream containing methane, components2components3and heavier hydrocarbon components, volatile residual gas fraction containing a major portion of the specified methane and components2and a relatively less volatile fraction containing a major portion of these components WITH3and heavier hydrocarbon components by processing the specified gas stream in one or more heat exchangers and/or expansion stages for the partial condensation of at least part of it and ensure that the at least first flow of steam and at least one liquid stream that contains3and lighter hydrocarbons, and direction, of at least one of these liquid streams containing3in the distillation column for separation of the specified fluid to the second patio, containing the major part of these components3and heavier hydrocarbon components, characterized in that the second steam flow is cooled sufficiently to condense at least part of and education in the condensed stream, the part of the said condensed stream is served to the specified distillation column at a top feed position of the raw material, at least part of the said first steam flow is subjected to close contact, at least part of the remaining portion of the specified condensed stream, at least one contacting device for education in the third stream of vapor and liquid stream that contains3specified fluid flow containing3served in specified distillation column as a second raw for her, at least part of the said third stream of steam is directed to the heat exchange with the specified second steam flow and ensure that the cooling in the first stage and then unload at least some of the listed third of the steam flow in the form specified volatile fraction of residual gas, and the quantity and temperature of the flows of raw materials in the Union upper temperature specified contact device and the specified distillation column at the level of the temperature, to get the main part of the above mentioned components3components and heavier hydrocarbons in the specified relatively less volatile fraction.

2. The method according to p. 1, characterized in that at least part of the specified fluid flow containing3is heated prior to its submission to the specified distillation column.

3. Method of separating a gas stream containing methane, components2components3components and heavier hydrocarbons, volatile residual gas fraction containing a major portion of the specified methane and components2and a relatively less volatile fraction containing a major portion of these components WITH3and heavier hydrocarbon components by processing the specified gas flow in one or more heat exchangers and/or expansion stages for the partial condensation of at least part of it and ensure that the at least first flow of steam and at least one liquid stream that contains3and lighter hydrocarbons, and direction, of at least one of these liquid streams containing3in the distillation column for separation ukazovatele less volatile fraction, containing the major part of these components3and heavier hydrocarbon components, characterized in that the second steam flow is cooled sufficiently to condense part of and education in the partially condensed stream specified partially condensed stream is divided to produce a third stream of vapor and a first liquid stream containing3at least the part of the said first liquid stream that contains3served in specified distillation column at a top feed position of raw materials, specified third stream of steam is cooled sufficiently to condense at least part of and education in the condensed stream, at least part of the said first steam flow is subjected to close contact, at least part of the specified condensed stream, at least one contacting device for the formation of the fourth steam flow and the second fluid stream containing3at least the part of the said second liquid stream containing3guide for heat exchange with the specified second steam flow leaving the upper area specified this thread pair, then the specified second liquid stream containing3served in specified distillation column as a second raw for her, at least a fourth part of the said flow of steam is directed to the heat exchange with the specified third steam flow and ensure that the cooling in the fourth stage, then unload at least some of the listed fourth of the steam flow as specified volatile fraction of residual gas, and the quantity and temperature of the flows of raw materials specified in the contact device and the specified distillation column are effective to maintain the upper temperature specified contact device and the specified distillation column at the level of the temperature, to get the main part of the above mentioned components3components and heavier hydrocarbons in the specified relatively less volatile fraction.

4. The method according to p. 3, characterized in that at least a part of the said second liquid stream containing3is heated to a direction for heat exchange with the specified second steam flow.

5. Method of separating a gas stream containing methane, components Stergiadou the main part of the specified methane and components2and a relatively less volatile fraction containing a major portion of these components WITH3and heavier hydrocarbon components by processing the specified gas flow in one or more heat exchangers and/or expansion stages for the partial condensation of at least part of it and ensure that the at least first flow of steam and at least one liquid stream that contains3and lighter hydrocarbons, and direction, of at least one of these liquid streams containing3in the distillation column for separation of the specified fluid to the second steam flow containing predominantly methane and components2and indicated relatively less volatile fraction containing a major portion of these components WITH3and heavier hydrocarbon components, characterized in that the second steam flow is cooled sufficiently to condense at least part of and education in the condensed stream, at least part of the said first steam flow is subjected to close contact, at least part of the specified condensed stream, at least one contatore, the part of the said liquid stream that contains3is heated and then fed to a specified distillation column at a top feed position of the raw material, at least part of the said third stream of steam is directed to the heat exchange with the specified second steam flow and ensure that the cooling in the first stage and then unload at least some of the listed third steam flow as specified volatile fraction of residual gas, and the quantity and temperature of the flows of raw materials specified in the contact device and the specified distillation column are effective to maintain the upper temperature specified contact device and the specified distillation column at the level of the temperature, to get the main part of the above mentioned components3components and heavier hydrocarbons in the specified relatively less volatile fraction.

6. A device for the separation of a gas containing methane, components2components3and heavier hydrocarbon components, volatile residual gas fraction containing a major portion of the specified methane and components2and relatively less LEUCO one or more means for heat exchange and/or funds for expansion, interconnected to provide at least one partially condensed gas stream and produce at least the first stream of steam and at least one liquid containing3and lighter hydrocarbons, and a distillation column for receiving at least one of the liquid streams containing3and to divide the specified stream to the second stream of steam containing predominantly methane and components2and indicated relatively less volatile fraction containing a major portion of these components WITH3and heavier hydrocarbon components, characterized in that it includes means of heat exchange associated with the specified distillation column, to obtain the second stream of steam and cool it sufficiently to condense at least part of and education in the condensed stream dividing means for receipt of said condensed stream and divide it into first and second streams of fluid associated with the specified distillation column to supply it specified the first fluid flow in the upper position feed, con, at least part of the first steam flow and mixing at least one contacting device, such contacting and separating means includes a separating means for separating vapor and liquid after contact in the specified contact device to produce a third stream of vapor and liquid stream that contains3, and is associated with the specified distillation column to supply it to the specified fluid flow containing3as the second source of raw materials and with the specified heat exchange direction, at least part of the third stream of steam for heat exchange with the specified second steam flow, and control means arranged to regulate the quantities and temperatures of the flows of raw materials specified in the contacting and separating means and the specified distillation column to maintain the upper temperature specified contacting and separating means and the distillation column at the level of temperature that can extract the main part of the components3and heavier components in the specified relatively less volatile fraction.

3and linked to the distillation column to supply the specified heated fluid stream containing3in specified distillation column as a second feedstock for her.

8. A device for the separation of a gas containing methane, components2components3and heavier hydrocarbon components, volatile residual gas fraction containing a major portion of the specified methane and components2and a relatively less volatile fraction containing a major portion of these components WITH3and heavier components containing one or more means for heat exchange and/or means for expanding, interconnected to provide at least one partially condensed gas stream and produce at least the first stream of steam and at least one liquid containing3and lighter hydrocarbons and a distillation column for receiving at least one of the liquid streams containing3and to divide the specified stream to the second stream of steam containing preimushestva components3and heavier hydrocarbon components, characterized in that it includes a first heat exchange associated with the specified distillation column, to obtain the second stream of steam and cool it sufficiently to partially condense and education in the partially condensed stream dividing means associated with a first heat exchange to obtain the partially condensed stream and divide it into the third flow of vapor and a first liquid stream containing3and with the specified distillation column to supply it, at least part of the fluid stream that contains3in the upper position of the feed, the second heat exchange associated with the specified separating means for receipt of said third stream of steam and cool it sufficiently to condense at least part of and education in the condensed stream, contacting and separating means to receive at least part of the condensed stream and at least part of the first steam flow and mixing, at meeba separating means for separating vapor and liquid after contact in the specified contact device for the formation of the fourth steam flow and the second fluid flow, contains3while specified first heat exchange associated with the specified contacting and separating means to receive at least part of the second liquid stream containing3and areas for heat exchange with the specified second steam flow leaving the upper area of the specified distillation columns, and cooling and partial condensation as a result of this second stream of steam and with the specified distillation column to supply it to the specified second liquid stream containing3as the second feedstock for her, and said contacting and separating means associated with the specified second heat exchange direction, at least part of the fourth flow of steam for heat exchange with the specified third steam flow, and control means arranged to regulate the quantities and temperatures of the flows of raw materials specified in the contacting and separating means and the specified distillation column to maintain the upper temperature specified contacting and separating means and the distillation column at the level of the temperature, Eitenne less volatile fraction.

9. The device under item 8, characterized in that said contacting and separating means connected with the third heat exchange, heating at least the part of the said second liquid stream containing3and associated with a first heat exchange for sending the said heated second stream of fluid containing3for heat exchange with the specified second steam flow leaving the upper area of the specified distillation columns.

10. A device for the separation of a gas containing methane, components2components3and heavier hydrocarbon components, volatile residual gas fraction containing a major portion of the specified methane and components2and a relatively less volatile fraction containing a major portion of these components WITH3and heavier components containing one or more means for heat exchange and/or means for expanding, interconnected to provide at least one partially condensed gas stream and produce at least first flow of steam, and at least one liquid containing3and lighter pleocoma3and to divide the specified stream to a second gas stream containing predominantly methane and components2and found relatively less volatile fraction containing a major portion of these components WITH3and heavier hydrocarbon components, characterized in that it includes a first heat exchange associated with the specified distillation column, to obtain the second stream of steam and cool it sufficiently to condense at least part of and education in the condensed stream, contacting and separating means to receive at least part of the condensed stream and at least part of the first steam flow and mixing at least one contacting device, but such contacting and separating means includes a separating means for separating vapor and liquid after contact in the specified contact device to produce a third stream of vapor and liquid stream that contains3the second heat exchange associated with the specified contacting and separating means for receiving, for crainey feed it specified the heated fluid stream, contains3in the upper position of the feed raw materials, such contacting and separating means connected with a first heat exchange direction, at least part of the third stream of steam for heat exchange with the specified second steam flow, and control means arranged to regulate the quantities and temperatures of the flows of raw materials specified in the contacting and separating means and the specified distillation column to maintain the upper temperature specified contacting and separating means and the distillation column at the level of temperature that can extract the main part of the components3and heavier components in the specified relatively less volatile fraction.

 

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