• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A process of and apparatus for liquefying a dry gas with low boiling point in a first circuit through heat exchange with a main refrigerating fluid in a second circuit itself pre-cooled to its at least partial liquefaction through heat exchange with an auxiliary refrigerating fluid in a third circuit, wherein, for a same amount of treated products, the required total compression input power for the refrigerating fluids is reduced by performing in said third circuit an intermediate condensation between the two last compression stages followed by a phase separation, the gaseous phase being compressed to a high pressure in the last compression stage whereas the liquid phase is compressed to a high pressure by a pump and recycled to a cryogenic heat exchanger for cooling the gas initially in the moist state thereby at least partially drying same.
    公开号:SU1355138A3
    申请号:SU803222450
    申请日:1980-12-11
    公开日:1987-11-23
    发明作者:Парадовски Анри；Каетани Энцо
    申请人:Компани Франсэз Д.Этюд Э Де Констрюксьон Текнип (Фирма)；Снампрогетти С,П.А.(Фирма)；
    IPC主号:
    专利说明:

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    (.r L111G1G) liquid phase 31) 1 Dropsy are likewise and see: 1 gcccc) t with ncprjoii part of CMt - inaitnoi o flow (timed doggimmeltshm gm cooled cold mm and ncyriiKoii.
    2. Onoooooooooooooooooooooooooooooooooooooooooooooooooooooooooooooooooooooo! 2. Onoooob on p. The invention relates to the method of cooling gas to a low temperature and especially liquefying natural or synthetic low boiling point sludge, such as, for example, a gas with a high content of methanol.
    The purpose of the invention is to increase efficiency by increasing energy efficiency and eliminating hydrate formation.
    FIG. 1 shows an embodiment of a method for liquefying a gas, for example natural gas, by condensing an auxiliary refrigerant at intermediate and high pressure and by throttling the latter at intermediate and low pressure; FIG. 2 shows a variant in which the auxiliary refrigerant is throttled at three different pressures — low, medium and intermediate; in FIG. 3, a variant with three different throttling pressures according to FIG. 2, in which the main refrigerant is cooled and liquefied, at least partially in two consecutive, stages through heat exchanges with the auxiliary refrigerant; Fig. 4 is a variant according to Fig. 2: P15 of pre-cooling of liquefied gas with an auxiliary refrigerant with throttling to an intermediate pressure; 5- option according to} 1o fig.Z of pre-cooling of liquefied gas together with an all-round refrigerant of this 1) ac1ir1 (second auxiliary foot on oh.pzhd (linego stream in internal
    isch o dag LG III ipprliliyut CLIOTHOT-st) (tupemi squeeze.
    3. (; ALARM) according to PG1.1 and 2, about tl and the fact that simultaneously with donor cooling and with liquefied gas, a reverse flow is organized from the first part of the mixed flow from its droplet-interim to the average pressure and the subsequent softening of it with medium pressure steam before compression.
    In this case, the space of the shell of the corresponding heat exchanger with the associated one, evaporation in this space.
    The lighter refrigerant may be, for example, the following multicomponent mixture, mol%:
    Lzot0-10
    Methane30-60
    Ethylene or
    ethane30-60
    Propylene, propane,
    butane and less volatile0-20
    The auxiliary refrigerant, which is heavier, may be, for example, the following multi-component mixture, mol%: Methane 0-15
    Ethylene or
    ethane30-65
    Propylene or
    propane 10-60
    Isobutane or
    butane and less
    volatile 0-30
    The method is carried out as follows.
    Liquefied gas, for example, natural, in a relatively dry state, flowing through pipeline 1 at a temperature of, for example, 20 ° C and absolute pressure, for example, about A5 bar passes through channel 2 of heat exchanger 3 for pre-cooling in it by heat exchange with light basic refrigerant
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    volume circulating p channel 4 of the same heat exchanger, in napraplen nin, opposite to the direction of gas flow in channel 2. The output from the heat exchanger 3 through pipe 5, the gas has a temperature of about and absolute pressure of about 44 bar, and then it passes through the processing device 6 , then going through pipeline 7 to the inlet of channel 8 in successive sections 9 and 10 of the heat exchanger 11, to be respectively fully liquefied and supercooled there as a result of heat exchange with the main refrigerant. At the exit of the heat exchanger 11 szh The compressed gas has a temperature of about -160 ° C and an absolute pressure of about 40 bar, then it expands in the throttle valve 12 and is transported via pipeline 13 to the place of preservation or storage of liquefied natural gas or to the place of processing or use of the latter.
    The main refrigerant is supplied completely in vapor or gaseous state at a temperature of about 5 ° C and a low absolute pressure, for example about 3 bar, to the first compression stage 14, from where it is pumped at intermediate pressure through the interstage cooling device 15 and to the second compression stage 16. which raises its pressure, keeping it in a gaseous state, to a high absolute pressure, for example about 30 bar, passing through the end cooling device 17, from where it exits, preferably remaining in the gaseous state, at a temperature of, for example, 35 ° C. Interstage and end cooling is carried out with an extraneous coolant. It then enters the channel 18 of the heat exchanger 19, where the main refrigerant is cooled as a result of heat exchange with the auxiliary refrigerant to at least partially be hedgehogs. The main refrigerant is at least partially condensed at a temperature of about -65 ° C and an absolute pressure of about 29 bar, leaves the heat exchanger 19 as a mixture of phases, respectively, gaseous and liquid, which are then separated in the separator 20. The gaseous phase is discharged through line 21 to
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    the section of the channel 22, which is located in section 9 of the heat exchanger 11, is liquefied there, then this liquefied part is supercooled in the section of the channel 22 placed in section 10 of the heat exchanger 11, from where this supercooled part goes through pipe 23 at a temperature of about -160 ° C and absolute pressure about 23 bar, then pass through throttle valve 24 for expansion. This expansion cools this part of the phase to a temperature of, for example, about. -163 ° C, lowering the absolute pressure, for example, to about 4 bar, then this expanded portion of the phase is led through conduit 25 to distribution unit 26, where the transversely divided portion of the phase is sprayed into the heat exchanger 11, into its annular space, forming a reverse flow. Thus, the main refrigerant flows in the form of a reverse flow (low pressure steam), washing the channels 8, 22 to 27 of the heat exchanger 11, while it continues to evaporate as a result of direct contact with the auxiliary refrigerant, and is counter-current to the streams respectively transported in these channels of the heat exchanger.
    Thus, the light primary refrigerant circulates through the following predetermined contour of the cooling cascade: compression stages 14 and 16 — heat exchanger 19 — heat exchanger 11 — heat exchanger 3 and again compression stages 14 and 16, etc.
    The liquid phase of the main refrigerant, separated in separator 20, is directed through conduit 28 to channel 27 of section II of the heat exchanger II, to be supercooled there to a temperature of about -135 ° C and have an absolute pressure of about 28 bar, and it leaves section 9 through the pipeline 29 to then pass through valve 30 for throttling. This cools this part of the phase to a temperature of about -133 ° C, lowering its pressure to 3.7 bar., Then the cross-flow is diverted through conduit 31 to distribution device 32, where it is sprayed into the internal space of the heat exchanger 11. This distributed part of the phase flows then in counterflow, i.e. and direction.
    51-3551.38
    brotherly direction of flow of flow of cold water ln di di sh h. tr to d a l ia pa dpém de l o p o from and n d gd zhu me about vr on others
    in the respective channels 8, 22 and 27, washing the latter in such a way that it continues to evaporate as a result of direct contact, and this low-pressure steam is mixed with the low-pressure vapor of the refrigerant flowing from the distribution device 26, washing the three channels of the heat exchanger 11 This direct contact between the reverse flow of low-pressure steam and the indicated flows in the heat exchanger channels causes heat exchange between them, thus producing, on the one hand, a vigorous subcooling of the liquefied gas and izhenie refrigerant circulating respectively in the channels 8 n 22, located in section 10, and, on the other hand, the liquefaction of streams in the respective channels arranged in sections 9 and transferred ohlazhd.enie liquid coolant circulating in the channel. 27 in the same: section 9.
    The fully evaporated main refrigerant leaving the heat exchanger 11 through the outlet 33 and the pipe 34 then passes through the heat exchanger 3 through channel 4, to the circulation in it in the direction opposite to the direction of flow of liquefied natural gas in channel 2, in order to cool the latter the result of heat exchange. The gaseous main refrigerant leaving the heat exchanger 3, for example, at a temperature and an absolute pressure of 3 bar, is then reabsorbed by the compression stage 14 in order to repeat the cooling cycle, forming a closed loop of the cooling cascade.
    Auxiliary refrigerant is sucked in a gaseous state, for example, at a temperature of about 30 ° C and a low absolute pressure of 3 bar by the first step 35 of compression and is compressed to an average pressure, then the passage through the interstage cooling unit 36, from where it is sucked in a gaseous state by the second to last step 37 compression, where it is reduced to an intermediate pressure, for example, about 20 bar. In the interstage cooler 38, the compressed auxiliary refrigerant condenses at least partially in the phase mixture, respectively
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    figurative and liquid1 at a temperature of, for example, about. Leaving the cooler 38, the auxiliary refrigerant is mixed with another part of it, evaporated for the most part, then undergoes separation in the separator 39. The gaseous phase is sucked by the third compression stage 40, where it is brought to high pressure, for example about 30 bar, and sent to the pipeline 41 The separated liquid phase is sucked by a pump 42, which raises its pressure to a high pressure, approximately equal to the pressure after the third stage 40 of compression, and directs this liquid phase, for example, at absolute At about 32 bar and a temperature of about into the injection pipe 43, where most of the discharge is through pipe 44 through valve 45 to pipe 41 to mix with the gaseous stream pumped by compression stage 40, while the other part is smaller The pipeline 43 is throttled in the liquid state (without a phase change) in the choke 46 to an intermediate pressure of 20 bar. The mixture of high-pressure phases, respectively, gaseous and liquid in the pipeline 41 then enters the end cooler 47 dp of liquefaction there in the majority. Interstage and end coolers work on an external heat carrier. The liquid thus liquefied largely leaves cooler 47 through conduit 48 and divides at two points 49 of the branch into two parts: one part flows through channel 50 of heat exchanger 19, where it is subsequently fully liquefied, then overcooled as a result of heat exchange at least at least part of her, i.e. when a back flow is formed, while the other part flowing through conduit 31 passes through choke 52 where it is choked to an intermediate pressure of about 20 bar, which causes its partial evaporation. The supercooled refrigerant in the channel 50 of the heat exchanger 19 leaves the latter through pipeline 53 at a temperature of about -63 ° C and an absolute pressure of about 28 bar and passes through the throttle
    71
    54 where it expands. This expansion cools it to a temperature of about -70 ° C, lowering its pressure to a pressure lower than intermediate, for example, 3.3 bar, then this stream enters the switchgear 55, where it is sprayed by nozzles in the internal space of the heat exchanger 19, forming the opposite flow. The return flow performs additional heat exchange with the current compressed in the last stage 17 of compressing the main refrigerant flowing in channel 18 and the flow of auxiliary refrigerant in channel 50, washing these two channels of flow in countercurrent at the same time. Thermal exchange occurs between the streams transported respectively in channels 18 and 50 and the return stream distributed in the interior of the heat exchanger 19, which continues to evaporate as a result of concomitant heating, while the corresponding streams in channels 18 and 46 are cooled, which causes at least partial liquefaction of the main refrigerant circulating in channel 18, and successively complete liquefaction and then overcooling of the auxiliary refrigerant circulating in channel 50. Auxiliary The refrigerant vaporized in the internal space of the heat exchanger 6 is discharged from the latter through the outlet 56 at a temperature of about 30 ° C and a pressure of about 3 bar, flowing through the pipe 57 to the inlet of the first stage 35. compressing, thus ensuring a repetition of the cooling cycle, t . closed loop cooling cascade. The choked liquid phase of the auxiliary refrigerant after droplets 46 is mixed at point 58 with a partially evaporated part of the stream coming out of droselles 52, after which this mixture of the gaseous and liquid phases passes through heat exchanger 59, where thermal exchange takes place between the auxiliary refrigerant and the liquefied moist natural gas, flowing through channel 60, circulating in it in the direction opposite to the direction of flow of the auxiliary refrigerant. Liquefied wet natural gas enters the heat exchanger 50 through the pipeline 61
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    388
    at a temperature of about 35 ° C and an absolute pressure of about 48 bar for additional pre-cooling and drying, then leaves the heat exchanger 59 through conduit 62 at a temperature of about 20 ° C and an absolute pressure of about 47 bar and in a relatively dry state to be dried even more, and then enters the inlet pipe 1 (its pressure then drops to 45 bar due to the loss of load incurred). In heat exchanger 59, the auxiliary refrigerant is heated as a result of heat exchange with liquefied moist natural gas, thus partially evaporated, and it leaves heat exchanger 59 at a temperature of about 30 ° C and pressure of 20 bar the auxiliary refrigerant stream after the penultimate stage 37 of compression and the cooler 38 so that this mixture, consisting respectively of the gaseous and liquid phases, returns to the separation stage in the separator 39 for the purpose of repeating the cascade azhdeni in a closed circuit. By recirculating the liquid portion of the auxiliary refrigerant at the high pressure created by the pump 42 in the pipe 43, it is possible to avoid the formation and precipitation of hydrates in
    liquefiable wet natural gas during its passage through the heat exchanger 59 due to maintaining the temperature of the auxiliary refrigerant, despite its throttling in the throttle 52 with respect to the liquid portion entering through the pipeline 43.
    The heat exchangers 11 and 19 consist, for example, of wound tube bundles, while the heat exchanger 3 is, for example, of plate type. The heat exchanger 19 may also be of the plate type.
    At the outlet of the throttles 54, the pipe 65 is connected to the evaporation channel 66 of the heat exchanger 19 located between the pipes 65 and 57. In the heat exchanger 19, an additional evaporation channel 67 is formed, the end of which is downstream connected via the pipe 68 to the suction port of the second compression stage 37, and its end is at the top of the junction
    91
    via pipe 69 with the output of another device for throttling, for example, throttle 70, whose inlet is connected via pipe 71 at intermediate point 72 of pipe 53 located between throttle 54 and channel 50, at the exit of interstage cooling device 36 between the first and second stages 35 and 37 compression pipe 73 is connected at an intermediate point 74 of pipe 68 between evaporation channel 67 and second compression stage 37.
    The quantitative molar composition of the heavy auxiliary refrigerant can be, for example, changed as follows,%:
    Methane0-10
    Ethylene or
    ethane30-70
    Propylene or
    propane 10-60
    Isobutane or
    normal butane
    and less volatile. hydrocarbons 0-20
    In this case, the supercooled liquid auxiliary refrigerant circulating in conduit 53 is divided at point 72 into two partial parallel streams, of which the first passes through the throttle 54 to expand in it, thus cooling to about -70 ° C and having absolute pressure up to 3 bar, then it passes through channel 66 for further evaporation in it due to heat exchange in countercurrent with the flows circulating respectively in channels 18 and 50, and leaves the heat exchanger 19 through pipe 57 at a temperature of about 3 0 C and pressure about 2.5 bar. Another partial flow, flowing through conduit 71, passes through choke 70, where it expands, reducing its pressure to 10 bar, then it passes through channel 67 for further evaporation in it due to heat exchange in countercurrent with refrigerants, respectively, primary and secondary, circulating respectively in channels 18 and 30. This other partial stream, completely evaporated, leaves channel 67 through conduit 68 at a temperature of about 30 ° C and a pressure of about 3 bar, corresponding to
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    The discharge pressure of the first stage 35 of compression in pipeline 73. At point 74, it mixes with the auxiliary refrigerant gas exiting from the interstage cooler 36, then the combined two gaseous streams are sucked by the second stage 37 of compression.
    Thus, in this embodiment, the auxiliary refrigerant evaporates at three different pressures, which respectively are the low pressure existing at the suction of the first compression stage 35, the average pressure between the first and second stages 35 and 37, and the intermediate pressure between the stages 37 and 40 squeeze.
    The main refrigerant can, instead of being subjected to single pre-cooling due to heat exchange with an auxiliary refrigerant in a single heat exchanger 19, is subjected to two successive cooling due to successive heat exchanges in two heat exchangers 75 and 76 in which the corresponding channels 77 and 78 of the main refrigerant are connected in series intermediate pipe 79 and a downstream end of the flow channel 78 is connected to pipe 80 leading to the separator 20. In this embodiment, the channel 81 of the first heat exchanger 75, while after point 72 the pipeline 53 is connected to the channel 82 located in the second heat exchanger 76, and is connected via pipe 83 to the entrance of the throttles 54. that the corresponding evaporations of the liquid auxiliary refrigerant, expanded to throttles 54 and 70 at two different pressures, respectively low and medium, continuously take place in two separate heat exchangers 75 and 76, pipelines 65 and 69 for d Corresponding partial streams of the expanded auxiliary refrigerant can here be connected to dispensing devices, for example, nozzles 84 and 85, respectively, going out to the internal spaces of heat exchangers 76 and 75, respectively.
    (although at least one or each of the pipes 65 and 69 may be connected to an evaporation channel located in the respective heat exchangers 76 and 75).
    The cooling streams (light main and heavy. Auxiliary) essentially each have the same quantitative and qualitative relative composition as in the previous case.
    The auxiliary refrigerant, which leaves the channel 81 of the heat exchanger 75 in the liquid supercooled state through the pipeline 53, has a temperature of about -10 ° C and an absolute pressure of about 29 bar. The expanded volumetric flow coming from the throttles 70 through conduit 69 has a temperature of about -1b and an absolute pressure of about 10 bar, this flow is distributed by the nozzles 85 into the inner space of the heat exchanger 75, where it continues to evaporate as a result of heat exchange to the contact in countercurrent with the corresponding flows circulating in the channels 77 and 81, and out through the opening 86 of the casing of this heat exchanger at a temperature of about 30 ° C and a pressure of about 9 bar. Another partially liquid supercooled auxiliary refrigerant stream, coming from point 72, passes through channel 82 to heat exchanger 76 to further overcool there, and leaves this flow channel through pipe 83 at about -65 ° C and absolute pressure. About 28 bar to then expand in throttle 54, thus having a lower temperature, e.g. about -70 ° C, 1L reduced absolute pressure (about 3 bar). This expanded partial flow is then distributed at point 7A into the interior of the heat exchanger 76, where it continues to evaporate as a result of heat exchange with the flows circulating in channels 78 and 82, respectively, thus cooling these flows even more. This second partial flow, evaporated in this way, leaves the internal space of the heat exchanger 76 through the outlet 87 in the heat exchanger casing 76, entering the pipeline 57 at a temperature of about -15 ° C
    and a low absolute movement of about 2.5 bar. The low pressure auxiliary refrigerant gas in line 57, which goes to the suction of the first stage 35, is cooler, i.e. the temperature is lower () than in the case of the previous embodiment (where its temperature is about 30 ° C). In this case, a constantly increasing amount of refrigerant is supplied to each compression stage at a corresponding pressure.
    A further embodiment differs from the previous one in that a pre-cooling cryogenic heat exchanger 88 is connected to a relatively dry liquefied natural gas, which (heat exchanger) is installed in the gas inlet pipe 1 in front of the gas-cooled cryogenic heat exchanger 3.
    5, the precooling heat exchanger 88, which is of a plate type, contains at least one passageway 89 for gas, connected at its end to
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    pipe 1 and its opposite end by means of connecting pipe 90 with the inlet of the channel 2 of the cryogenic heat exchanger 3 for gas cooling. In addition, the heat exchanger 88 contains at least one channel 91 and one evaporation channel 92 for an auxiliary refrigerant, located at least approximately parallel to the direction of the channel 82 and mutually connecting in series. The channel 91 is connected to its input end by a pipe 93 with an intermediate point 94 of a pipe 43 located between channel 50 and a point 49. The opposite end of the channel 91 is connected by a pipe 95 to an inlet of a drossel-type expander 96, the outlet of which is connected the inlet of the evaporation channel 92, the opposite end of which is connected by a pipe 98 to a suction port of the second compression stage 38, at intermediate points 73 and 99 of this pipe 98, branches respectively pipes the cable 73 at the outlet of the interstage cooling device 36 and the pipeline 68.
    131
    The refrigerants, respectively, light basic and heavy auxiliary, have here, for example, the same essentially relative qualitative and quantitative compositions, that and the corresponding refrigerants in the embodiment shown in FIG. 2,
    The liquefied gas is in a relatively dry state at about 20 ° C and an absolute pressure of about 45 bar through pipe 1 and passes through the channel 89 of the pre-cooling heat exchanger 88, where this gas is pre-cooled, having a lower temperature, for example about -15 ° C (at an appropriate pressure, e.g. about 44.5 bar), as a result of heat exchange with an auxiliary refrigerant flowing in the same pre-cooling heat exchanger 88. The gas thus pre-cooled enters through conduit 90 to a cryogenic cooling exchanger 3, starting from which its physical and thermodynamic development is the same as described.
    Part of the liquefied auxiliary refrigerant, which enters at least mostly through pipeline 48, after point 49 is withdrawn at point 94 by pipeline 93 and passes through channel 91 of precooling exchanger 88, where this part is successively fully liquefied and then supercooled as a result of heat exchange at least part of her. This liquid supercooled part leaves channel 91 through conduit 95, having a temperature of about -15 ° C and an absolute pressure of about 29 bar, then passes through choke 96, where it undergoes expansion, which cools it to a temperature of about -20 ° C, lowering its absolute pressure up to about 10 bar. The part of the auxiliary refrigerant expanded in this way exits the throttles 96 through conduit 97 das passage through channel 92, where this part completely evaporates as a result of heat exchange in opposition to the streams circulating respectively in channel 89 and in channel 91, which causes on the one hand, preliminary additional cooling of liquefied natural hectares
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    channel 89 and, on the other hand, complete liquefaction and subcooling of part of the auxiliary refrigerant circulating in channel 91.
    Thus, the fully evaporated part of the auxiliary refrigerant leaves the heat exchanger 88 through a pipe 98 with a temperature of about and an average pressure of about 9 bar, to be then mixed at points 99 and 74 with the evaporated parts of the auxiliary refrigerant flowing through pipelines 68 and 73, respectively then the flows of the gaseous and auxiliary refrigerants combined in this manner are sucked in by the compression stage 37.
    This diagram (Fig. 4) demonstrates the separation of the compression power between the main refrigerant circuit and the auxiliary refrigerant circuit, and it may be beneficial to load one of these two circuits more than the other. In this case, the compression power is the same in these two circuits, but the auxiliary refrigerant circuit, for example, is more loaded than in the embodiment shown in FIG. 2. As an example, the circuit according to Fig. 4 may contain a separate drive for compression stage 14, a separate drive for compression stage 15, a separate drive dp of compression stage 35 and a common drive dp of two compression stages 37 and 40 (which are then mechanically connected using corresponding shafts).
    The formed channel 92 in the precooling heat exchanger 8S can be replaced if necessary by the internal space bounded by the casing or chamber of the heat exchanger 88, and then the pipe 97 is connected to the distribution device by means of nozzles installed in the heat exchanger and directly that the auxiliary refrigerant flows in this internal space in counterflow with respect to the flows, respectively transported in channels 89 and 91, ohms and the latter by virtue of the forward contact.
    The scheme presented in figure 5 ,. follows from the diagram in FIG. 3 and differs from the latter by the addition of the cree
    151
    4, but in this case the plate-type heat exchanger in FIG. 4 is replaced by a heat exchanger in the form of twisted tube bundles. The auxiliary refrigerant expanded to medium pressure, distributed in the internal space of the heat exchanger 88 by the switchgear 100, then flows in the direction opposite to the general flow direction (i.e., the return flow is organized) of the respective flows in channels 89 and 91, washing the last My contact, where the heat exchange continues to evaporate the flow along with the accompanying cooling of liquefied natural gas in the canap 89 and the auxiliary refrigerant in the channel 91, the auxiliary refrigerant, thus completely (i.e., medium pressure steam) in the internal space of the heat exchanger 88, leaves the latter through the opening 101 in the shell

    3816
    heat exchanger 88 and then transported through conduit 98, as described. Relatively dry natural gas enters here via conduit 90 at a temperature of about 20 ° C and an absolute pressure of about 46 bar, and it is further cooled in the heat exchanger 88 to a temperature of, for example, -15 ° C at a pressure of about 45 bar.
    The reverse flow is then mixed with steam entering the second compression stage 37.
    Saving energy in this method arises due to the fact that in the auxiliary refrigerant cascade not all of its flow is compressed, but parts of it in different stages of compression, and the total power consumption decreases. In addition, the improved energy cycle used in the process makes it possible to more fully dry and cool the liquefiable gas, while preventing the formation of hydrates in it.
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    Editor S.Pekar Tehred L.Serdyukova
    Order 5720/58 Circulation 476Subscription
    VNNIBI State Committee of the USSR
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    - -.-.- - - - - --- - ---- - - - - - - - - -
    Production and printing company, Uzhgorod, Projecto st., 4
    Proofreader S. Shekmar
    权利要求:
    Claims (3)
    [1]
    1 . METHOD FOR GAS LIQUIDING with a low boiling point by heat exchange with at least part of the light main refrigerant stream, pre-cooled at least until it is partially liquefied by heat exchange with heavy, auxiliary refrigerant, while the auxiliary and main refrigerant flows form a cooling stage and consist of a multi-component mixtures of gases with correspondingly decreasing volatility, the circulation of each refrigerant is carried out in closed circuits, where refrigerants in a gaseous state are followed they are compressed in several stages with increasing pressure and interstage and end cooling and partial condensation using an external coolant, cooled with complete liquefaction and. supercooling due to the formation of a return flow of refrigerant that has already been cooled and throttled to low pressure while simultaneously exchanging the main and auxiliary refrigerants with the liquefied gas stream and the main refrigerant stream for at least partial liquefaction, after which the resulting low pressure refrigerant vapor is again compressed , the liquefied gas is initially cooled and dried by heat exchange with a stream of low pressure steam, characterized in that, in order to increase the efficiency ktivnosti method by increasing the energy efficiency and elimination of hydrate formation, compression auxiliary refrigerant performed with a gradual increase in its amount from stage to stage before compressing the entire stream, wherein after the penultimate stage stream is separated into liquid and gaseous phases which 1 discord is compressed and a portion the liquid phase after throttling is mixed with the gas phase and the resulting mixed stream after cooling with an external heat carrier is divided into two parts, the first of which is throttled to intermediate pressure, they are sent for additional preliminary cooling and drying of the liquefied gas and returned to the separation stage, and the second is cooled and liquefied by the formation of a reverse flow already cooled and. throttled to a pressure lower than the intermediate part of the refrigerant with simultaneous additional heat exchange with the flow of the main refrigerant compressed in the last stage, and the rest from SU „” 1355138> СН
    Π 5 separated vein phases are throttled and mixed with the first part of the mixed stream before additional cooling and drying.
    [2]
    2. The method according to claim 1, with the exception that when cooling and liquefying the second part of the mixed stream, the reverse stream is separated and throttled, respectively, to a low, to an average, but lower intermediate pressure, after whereby the resulting low and medium pressure steam is sent to the corresponding compression stages.
    [3]
    3. The method according to claims 1 and 2, characterized in that at the same time as additional cooling and drying of the liquefied gas, a return stream is organized from the first part of the mixed stream with its throttling to medium pressure and its subsequent mixing with medium pressure steam before compression.
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    US4303427A|1981-12-01|Cascade multicomponent cooling method for liquefying natural gas
    JPH0627618B2|1994-04-13|Method and apparatus for cooling and liquefying at least one low boiling point gas such as natural gas
    RU2499962C2|2013-11-27|Method and device to cool and/or liquefy hydrocarbon flow
    BR0315076B1|2014-11-04|Process and apparatus for liquefying natural gas
    US20050005635A1|2005-01-13|Plant and process for liquefying natural gas
    RU2005118106A|2006-01-27|IMPROVED METHANE INSTANT EVAPORATION SYSTEM TO REDUCE NATURAL GAS
    KR101955092B1|2019-03-06|Liquefaction method and system
    同族专利:
    公开号 | 公开日
    CA1142847A|1983-03-15|
    FR2471566B1|1986-09-05|
    FR2471566A1|1981-06-19|
    GB2067734A|1981-07-30|
    EG17909A|1991-06-30|
    DZ255A1|2004-09-13|
    BE886593A|1981-06-11|
    US4339253A|1982-07-13|
    NO154473B|1986-06-16|
    ES8200469A1|1981-11-01|
    NL189375C|1993-03-16|
    MY8600511A|1986-12-31|
    AU6531880A|1981-06-18|
    JPS56100279A|1981-08-12|
    DE3046549C2|1994-05-05|
    NL8006736A|1981-07-16|
    AU536389B2|1984-05-03|
    IN155149B|1985-01-05|
    IT1210012B|1989-09-06|
    DE3046549A1|1981-08-27|
    OA06667A|1981-09-30|
    IT8046911D0|1980-12-12|
    ES497706A0|1981-11-01|
    NO154473C|1986-09-24|
    AR228349A1|1983-02-28|
    NO803741L|1981-09-15|
    JPH0147718B2|1989-10-16|
    NL189375B|1992-10-16|
    GB2067734B|1983-11-30|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR7930489A|FR2471566B1|1979-12-12|1979-12-12|METHOD AND SYSTEM FOR LIQUEFACTION OF A LOW-BOILING GAS|
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