• 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:
    La présente invention concerne un procédé et un appareil de liquéfaction d'un gaz à bas point d'ébullition, tel que du gaz naturel, par échange de chaleur avec un fluide réfrigérant, à plusieurs composants. Selon l'invention, la phase vapeur du fluide réfrigérant principal, condensée et sous-refroidie est détendue, en une fois, à au moins une première pression, et la phase liquide du fluide réfrigérant principal sous-refroidie est détendue, en une fois, à au moins une deuxième pression, différente de ladite première pression. La présente invention s'applique notamment à la liquéfaction du gaz naturel.
    公开号:SU1627097A3
    申请号:SU843737939
    申请日:1984-05-04
    公开日:1991-02-07
    发明作者:Парадовски Анри；Лерукс Дидье
    申请人:Компани Франсэз Дъэтюд Э Де Констрюксьон "Текнип" (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods for cooling and liquefying at least one gas with a low boiling point, such as, for example, natural gas, or any mixture of gases containing at least one gas with a low boiling point.
    The purpose of the invention is to reduce energy consumption and increase thermodynamic efficiency when using plate heat exchangers.
    FIG. 1 shows a diagram of a device for cooling and liquefying a low boiling point eye, such as, for example, natural gas, FIG. 2 is a diagram of a cryogenic heat exchanger of the main cooling fluid circuit, first variant 1, FIG. 3 - then ЖР, the second option | in fig. 4th, third option; in fig. 5 is a diagram of the proposed device, option; in fig. 6 is a diagram of the auxiliary cooling circuit, option.
    An apparatus for implementing the method (FIG. 1) contains an open circuit 1 of a liquefiable gas, a closed loop 2 of the main coolant, a closed loop 3 of an auxiliary cooling fluid. The closed contours of the main and auxiliary coolants are symbolically limited and enclosed in a rectangular frame indicated by a dash-dotted line, and the path of movement of the liquefiable gas a is indicated by a solid thick line. The liquefied gas circuit 1 and the main cooling fluid circuit 2 are thermally coupled to each other by means of common cryogenic heat exchangers 4 and 5., gas liquefaction and subcooling and gas pre-cooling. The circuits 2 and 3 of the main coolant and the auxiliary coolant are interconnected by means of at least one common cryogenic pre-cooling heat exchanger 6 and at least partially liquefying the main coolant.
    Open loop 1 of liquefiable gas includes a supply pipe 7 to the pre-cooling heat exchanger 5 connected to at least one internal channel 8 of this heat exchanger, the output of which is connected via a pipe 9 to an facultatively installed gas treatment apparatus 10, for example to extract ethane. Thus, it is possible to provide for the installation of other gas processing apparatuses, in particular, an apparatus for extracting nitrogen can be provided at the level of the cryogenic heat exchanger 4. The output of the apparatus 10 through the pipe 11 is connected to the inlet of the heat exchanger 4.
    The branch 12 of the pipe 7 is connected to the channel 13 of the removal of part of the liquefied gas in a cryogenic heat exchanger 6 of the auxiliary cooling liquid circuit, the output of which
    dinene through pipe 14 to the pipe 11 installed before entering the heat exchanger 4. The pipe 11 is connected to the internal discharge channel 15 passing through a cryogenic heat exchanger 4. The rear end of the channel 15 at the exit of the heat exchanger 4 is connected to the pipe 16 of the liquefied gas, which is installed at least one expansion body 17, for example an expansion valve.
    Closed loop 2 contains a main coolant, which is a mixture of several components, at least most of which are hydrocarbons. The relative molar composition of this coolant may, for example, be as follows, /.
    Nitrogen 0-2
    Methane35-55
    Ethylene or ethane 28-65
    Propylene or
    propane 0-15
    In the coolant circulation direction, circuit 2 includes successively the first compressor 18 and the second compressor 19 for compressing the coolant in a gaseous state, each driven by its own engine or by a common engine. In the second case, their shafts are mechanically interconnected. Compressors 18 and 19 are connected in series with heat exchanger-cooler 20, in which cooling fluid preferably comes in from the outside and can be water or cooled air. The heat exchanger-cooler 20 is connected to a compressor 21 by a compressor 22. Compressors 22 and 23 can be driven by a common engine, an engine that drives compressors 18 and 19, or each has its own engine Compressors 22 and 23 are connected in series to at least one intercooler 24, the cooling fluid into which is preferably supplied from the outside and may, for example, be water or cooled air. The output of the compressor 23 through the pipe 25 and through the heat exchanger-cooler 26 (the cooling fluid which is preferably supplied from the outside and may be water or cooled air) is connected to the inlet of the heat exchanger 6, or rather to one of the internal channels 27. Cryogenic heat exchanger 6 of the circuit The auxiliary coolant is preferably a plate heat exchanger. At the outlet of the heat exchanger 6, the rear end of its internal channel 27 is connected via pipe 28 to at least one phase separator 29. The liquid collection chamber of this phase separator is connected via pipe 30 to the inlet of the heat exchanger 4, and more precisely to the front end of at least one channel 31 inside the heat exchanger 4 in the same direction as the internal channel 15, through which liquefied gas flows. At the outlet of the heat exchanger 4, the internal channel 31 is divided into two outlet channels 32 and 33 connected to the inputs of the expansion organon 34 and 35, respectively. To the exit of each organ 34 and 35 of the throat are connected to D1
    Units 36 and 37, passing inside the cryogenic heat exchanger 4 in the same direction as the internal channel 15 of liquefied gas and the internal channel 31, but countercurrent.
    The vapor collection chamber of the phaeo-separator 29 is connected to the inlet of the cryogenic heat exchanger 4 through the tube 38, and more specifically with the front end of at least one of its internal channel 39 running parallel to the channels 15 and 31. The rear end of the channel 39 at the exit of the heat exchanger 4 is divided into two channels 40 and 41 connected to the inputs of extension organs 42 and 43. The outlets of expansion units 42 and 43 are connected to channels 44 and 45, passing inside the cryogenic heat exchanger 4 in the same direction as channels 15, 31, 36, 37 and 39.
    The cryogenic heat exchanger 4 of the circuit 2 of the main coolant is a plate heat exchanger, the contents of the various cells for each liquid and gas involved in heat exchange, namely liquefied gas, liquid or vapor phase or fraction of the main coolant partially condensed, as well as fractions obtained and previous after expansion at various pressure levels. After exiting the cryogenic heat exchanger 4, the channels 36 and 44 for withdrawing the main coolant fractions brought to the same pressure, for example, to an average pressure of about 1.5-3 bar, are connected to one channel 46, which can pass through heat exchanger 5 for pre-cooling the liquefied gas by countercurrent. The rear end of the channel 46 is connected to the suction inlet of the compressor 19. After exiting the cryogenic heat exchanger 4, the channels 37 and 45 for withdrawing the main coolant fractions brought to the same pressure, for example low pressure, are less than 1 bar. , the rear end of which goes into the suction port of the compressor 18.
    Loop 3 contains an auxiliary coolant, preferably a mixture of exclusively hydrocarbons, which has
    an example, the following relative molar composition, 2:
    Ethylene or ethane 30-70 Propylene or propane 70-30 In the direction of liquid pressure, closed loop 3 of auxiliary coolant contains the following successive elements: the first compressor 48 and the second compressor 49 with a heat exchanger-cooler
    50 and a third compressor 51 with a condenser 52 and a subcooler 53, each driven by its own engine or at least one for at least two compressors by the engine. In the second case, the compressor shafts are mechanically connected. The outlet of the second compressor 49 through pipe 54 is connected to the inlet or suction port of the third compressor
    51 through a heat exchanger-cooler, the refrigerant in which is supplied mainly from the outside and is, for example, water or cooled air. The outlet of the third compressor 51 through the pipe 55 is connected to the condenser 52, the output
    which through pipe 56 is connected to the subcooler 53.
    The subcooled outlet 53 is connected via pipe 57 to a cryogenic heat exchanger 6, which may be a plate heat exchanger, and more specifically, to the front end of channel 58 passing through heat exchanger 6 in a direction parallel to the direction of channels 1 3 and 27 of liquefiable gas and main coolant, respectively .
    The channel 58 for withdrawing the auxiliary coolant to the cryogenic heat exchanger 6 has, for example, three
    branches 59-61 provided in heat exchanger 6 at three different levels. Branches 59-61 are each associated with one expansion member 62-64, respectively, the outlets of which are connected to separators 65-67 of vapor / liquid phases. In all three cases, the liquid collection chambers of separators 65-67 are connected via pipes 68-70 to the inlet of the cryogenic heat exchanger 6, or more precisely, with the front ends of the channels 71-73 passing inside the cryogenic heat exchanger 6 in a direction approximately parallel to the direction of the outlet channel 13
    liquefiable gas, channel 27 for removal of the main coolant and channel 1 for removal of the auxiliary cooling liquid before expansion. The vapor collection chambers of each separator 65-67 are connected via pipes 74-76 to the inlet of a cryogenic heat exchanger 6, or more precisely, with the front ends of channels 77-79 that pass inside the cryogenic heat exchanger 6 in the same direction as the other channels 13 , 27 and 58. At the exit of the heat exchanger 6, the channels 71 and 77, 72 and 78, 73 and 79 are connected in pairs in one channel 80-82, respectively. The outlet channel 82 is connected to the suction inlet of the compressor 48, the outlet channel 81 is connected to the suction inlet of the compressor 49, and the outlet channel 80 is connected to the suction inlet of the compressor 51. The installation (in accordance with the options in FIGS. 1-5) further comprises organs 83 and 84, pipes 85 and 86, separator 87 and pipes 88-92.
    Contour 1 works as follows. A liquefied gas, such as natural gas, supplied through pipe 7 at a temperature of + 20 ° C and under pressure, for example, 42.5 bar, passes through channel 8 of the heat exchanger 5, where it is pre-cooled by heat exchange with the main coolant state after expansion in a cryogenic heat exchanger 4 and circulating in channel 46 in the direction opposite to the direction of gas movement in channel 8. Exit from heat exchanger 5 through pipe 9, the gas already has a temperature of -45 ° C and a pressure of 42 bar. It then passes through the treatment apparatus 10 and through the pipe 11 enters the inlet of the channel 15 of the plate heat exchanger 4, where it is finally liquefied and then supercooled due to heat exchange with the main coolant. After exiting the heat exchanger 4, the liquefied gas has a temperature of -154 ° C and a pressure of 41.5 bar. Thereafter, it expands in the expander body 17 and is transported to the place of its processing or use.
    Part of the liquefied gas can also be pre-cooled by heat exchange with auxiliary coolant in a cryogenic
    five
    0 d $
    0
    five
    heat exchanger 6, after which this part is connected to the main mass of liquefied gas before it is fed to the cryogenic heat exchanger 4.
    Circuit 2 main coolant works as follows. A part of the main coolant, brought to a low pressure, is sucked in a gaseous state at a temperature of -5 ° C and a pressure of 0.08 bar by the first compressor 18, which brings its pressure to 2 bar and the temperature to 10 ° C, then it is sucked in by the second the compressor 19 simultaneously with a part of the main coolant, the pressure of which is adjusted to an average of 2 bar and the temperature to 10 C. The entire volume of liquid is brought to the temperature and to the pressure of 6.5 bar in the compressor 19, then passes through the heat exchanger-cooler 20 where the temperature is hydrochloric coolant decreases, e.g., to 15 ° C. Through the pipe 21, the liquid enters the suction inlet of the compressor 22, passes through the intercooler 24, is compressed in the compressor 23 and passes through the pipe 25 into the heat exchanger-cooler 26. At the outlet of the latter, the main coolant has a temperature of 15 ° C and a pressure of 27.4 bar. It then enters the channel 27 of the cryogenic heat exchanger 6, where the main cooling fluid is cooled by heat exchange with the secondary coolant and partially liquefied.
    Thus, the condensed main coolant has a temperature of -50 ° C and a pressure of 26.5 bar, exits the heat exchanger 6 as a mixture of gas and liquid phases, which are then separated in the phase separator 29. The gas phase flows through the pipe 38 into the channel 39 section located in the cryogenic heat exchanger 4, where it is liquefied and supercooled to a temperature. The part of this liquefied and supercooled gas phase passes through channel 41 and expands in expansion chamber 43 to a pressure of 0.3 bar, and its temperature is -156 ° C. At the exit of the channel 45 of this fraction of the liquefied and supercooled gas phase, its temperature and pressure are respectively -52 ° C and
    at 1
    0.08 bar. Another part of the liquefied and supercooled gas phase passes through the channel 40 and is brought to the pressure of 2.3 bar and a temperature of -153 ° C in the expansion body 42. At the exit of this fraction from the channel 44 of the heat exchanger 4, the temperature and pressure conditions are, for example, as follows: -152 ° C and 2.10 bar.
    The liquid phase of the main coolant from the phase separator 29 through the pipe 30 enters the channel 31 of the cryogenic heat exchanger 4, where it is supercooled to a temperature of -154 ° and its pressure is adjusted to 26 bar. A part of the supercooled liquid phase of the main coolant passes through the expansion body 35, where its pressure decreases to about 0.3 bar, while another part of the supercooled liquid phase passes through channel 33 to the expansion body 34, after which its pressure is 2 , 3 bar, and temperature -153 ° С. After passing through channels 37 and 36, respectively, the first and second parts of the liquid phase of the main coolant have the following (no pressure and temperature conditions: -52 ° C and 0.08 bar; -52 ° G and 2.10 6aj, respectively.
    Thus, the first part of the vapor phase of the main coolant after condensation and supercooling is adjusted to perlipose pressure, the second part is adjusted to the second pressure, the first part of the liquid phase of the main coolant is reduced to the specified first pressure after supercooling, and the second part is adjusted to the specified second pressure. The vapor and liquid phases can be divided into the desired number of parts, for example three or more, and the pressure to which the liquid phase is brought corresponds to the pressure to which the corresponding part of the vapor phase is brought. After evaporation, the first portions of the phases of vapor and liquid are mixed, the second portions of the phases of vapor and liquid are also mixed.
    The second possibility is to mix the first parts of the vapor and liquid phases and to mix the second parts of the vapor and liquid phases after expansion, but before evaporation (Fig. 5).
    Part of the main coolant evaporating at low pressure
    7 04
    through the channel 47 enters the suction inlet of the compressor 18, -i then as the second part of the main cooling-. The vapor of the liquid evaporating at medium pressure passes through the channel 46, the heat exchanger 5 of the preliminary cooling of the liquefied gas and enters the intake port of the compressor 19.
    Contour 3 auxiliary coolant works as follows. The auxiliary cooling fluid in the gaseous state comes out from the compressors 48, 49 and 51, having a temperature of + 46 ° C and a pressure of 16 bar. After passing through the condenser 52 and the subcooler 53, the auxiliary cooling liquid has a temperature of + 13 ° C and pressure
    15.1 bar. The part of the auxiliary coolant passing through the branch 59 has a temperature of 0 ° D and a pressure of 15 bar. After expanding into
    5 of the expansion body 62, the temperature decreases to -6.5 ° C, the pressure drops to 8.5 bar. The vapor and liquid phases thus obtained are separated in the separator 65 and supplied to the cryogenic heat exchanger 6 through channels 77 and 71 for heat exchange with fluids flowing through channels 13, 27 and 58 through the heat exchanger 6.
    Since the vapor and liquid phases are mixed after exiting the heat exchanger 6, the temperature and pressure conditions of the auxiliary cooling liquid are as follows: about 11 ° C and 8.5 bar. This part of the auxiliary coolant is supplied to the intake port of the compressor 51 through the channel 80 and the pipe 54.
    Conditions of temperature and pressure of the second part of the auxiliary coolant 5 Liquid, flowing through the branch 60, -25 ° C and 14.5 bar, respectively. After expansion in expansion chamber 63, the temperature drops to -29 ° C and pressure to 4 bar. The phases of vapor and liquid thus obtained flow through channels 78 and 72, respectively, into heat exchanger 6, where they participate in heat exchange with other liquids flowing through this heat exchanger 6, and then are mixed together after leaving heat exchanger 6 in channel 81. Condition temperature and pressure of this part of the auxiliary coolant
    five
    0
    five
     and 3.9 bar, respectively. This part of the auxiliary coolant enters the suction port of the compressor 49.
    The third part of the auxiliary coolant passes through the branch 61, having a temperature of -50 C, and a pressure of 14.2 bar. After expansion in expansion body 64, the temperature and pressure conditions are changed as follows: -54 ° C and 1.1 bar. The phases of vapor and liquid thus obtained are separated in separator 67 and through channels 73 and 79 enter the heat exchanger 6, where they participate in heat exchange with other liquids circulating there. After exiting the heat exchanger 6 and mixing these phases, the vapor and liquid have a temperature of -28 ° C and a pressure of 0.90 bar. The third part of the auxiliary coolant is supplied to the suction inlet of the compressor 48 through the channel 82.
    FIG. 2 shows the part of the device circled in FIG. 1 by a dash-dotted line. In this embodiment, the phase of the main cooling steam of the liquid after condensation and supercooling in the heat exchanger 4 is brought to the first pressure at a time in the expansion body 83. The liquid phase of the main coolant after supercooling in the heat exchanger 4 is brought up at a single time in the expansion unit 84 to a second pressure different from the first pressure. The phase of steam brought, for example, to a low pressure of less than 1 bar, passes through the heat exchanger 4, pipe 85 and enters the suction port of the first compressor 18, the liquid phase of the main coolant brought to medium pressure (for example, 1.5-3 bar), passes through the heat exchanger 4, the pipe 86 and enters the suction port of the second compressor 19. Thus, the device for cooling and liquefying gas with a low boiling point, such as, for example, natural gas, is presented in. FIG. 2, works similarly to the device presented in figure 1.
    FIG. 3 shows another variant of the construction of this part of the device (marked by a dotted line in FIG. 1). In this case, after expanding the condensed and n 0
    0
    five
    0
    the cooled phase, the steam in expansion chamber 83 and the resulting gaseous and liquid phases are separated in separator 87, and then re-passed, but in countercurrent through a cryogenic heat exchanger 4. After evaporation, both phases are mixed in a pipe 89 connected to the suction inlet of compressor 18. Therefore, in this case, the vapor phase is brought to a low pressure.
    The supercooled liquid phase of the main coolant expands 5 in the expansion body 84 and flows countercurrent through the heat exchanger 4, enters the pipe 90 and then into the suction inlet of the compressor 19. After leaving the separator 87, the phase may not pass through the heat exchanger 4 again into pipe 89.
    FIG. 6 shows the use of the device of this embodiment in the auxiliary coolant circuit. In this case, pipes 74-76, coming from the vapor collection chambers of separators 65-67, are connected directly to channels 80-82; mine heat exchanger 6.
    FIG. 4 shows a variant of the construction of a part of the device highlighted in FIG. 1 by a dash-dotted line and similar to the variant shown in FIG. In this case, each of the elements of the expansion bodies OF and 84, instead of being at the outlet of the heat exchanger 4, can be installed anywhere along the heat exchanger 4 in the direction of flow of various liquids. Thus, the circulation channel 31 of the liquid phase of the main coolant does not pass through the entire heat exchanger e 4. This allows expansion at different temperature levels, in which case the temperature may be higher after the valve passes. The expansion movement in accordance with the temperature gradient corresponds to the expansion body movement along the heat exchanger in the direction. flow of fluids.
    FIG. 5 shows a variant of the construction of the device in which the first parts of the vapor and liquid phases are mixed and the second parts of the vapor and liquid phases are mixed after expansion in expansion 5
    0
    0
    five
    13if
    body bodies 83 and 84, respectively, but in front of their direction in countercurrent to the heat exchanger 4.
    Example. The cooling and liquefaction of any natural gas is carried out in the following conditions: temperature 20 ° C, pressure 42.44 bar, mass flow rate, 34.408 kg / h.
    Chemical composition in molar percentage - Nz 0.36; G 93.06, Cr 4.08, G j 1.67, G4 0.83.
    Before the final expansion device, liquefied gas is obtained under the following conditions: temperature 153.7 ° C, pressure 41.44 bar.
    7 (Yu,
    The mass split and the sea, 1, n are identical to the depressed type.
    When calculating popuzhat slozhuya indicators
    Main cooling cycle. Molar composition,%: G, 40, G2 50, G3 10. The molar percentage ratio of the vaporizer liquid in the phase separator is 29:20.
    The distribution of the liquid and supercooled fractions of the main refrigerant, between the two ypoin, is determined by
    as
    molar flow rate of main refrigerant
    in channel 37
     molar flow rate of main refrigerant in channel 31
    molar flow rate of main refrigerant
    in channel 44
    molar flow rate of main refrigerant in duct 39 of heat exchanger 4
    R, 0.50 and R2 037
    Mass flow 408563 kg / h. The compressor suction pressure is 18 0.03 bar. The suction pressure of the compressor is 19.1, 95 bar.
    Power, kW: compressors 18 and 19-19256, compressors 22 and 23-19516, a total of 38772. The ratio of the amounts of heat exchanged at average temperatures of 67841400x10 J / / {h (° C) for heat exchanger 4.
    Auxiliary cooling cycle. Molar composition of auxiliary refrigerant,%: G, 240, SdBO, mass flow rate 600472 kg / h. The power of the compressors is 48, 49 and 51-17021 kW.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    A method of cooling and liquefying a gas with a low boiling point, mainly natural, including heat exchange of a gas with at least a part of the main multi-component refrigerant that is pre-cooled to at least partial liquefaction by heat exchange with an auxiliary multi-component refrigerant, circulating each refrigerant in a separate closed loop, in which it is consistent
    subjected to one compression of the gaseous state, at least one pre-cooling with at least partial condensation, separation of the resulting liquid and vapor Lase, at least
    one cooling with full liquefaction, one undercooling and expansion, subsequent return to evaporation by recuperative heat exchange in countercurrent with gas, mixing steam and preferably transferred to the vapor phase of the liquid phase of the auxiliary refrigerant, feeding the mixture for compression, while part of the liquefied gas is pre-cooled simultaneously with main refrigerant by heat exchange with an auxiliary refrigerant, and the main and auxiliary refrigerants form a cooling cascade, which is different in that Reductions of energy consumption and increase the thermodynamic efficiency in the use of plate heat exchangers, liquid and vapor phase wasps
    After cooling in a plate heat exchanger, each refrigerant is divided into at least two streams, reducing the pressure of one of the steam and liquid streams at a time.
    15162709716
    phases up to a single value equal to the pressure- ™ in the vapor and liquid phases up to a single generation of one compression stage, and for one value equal to the pressure another time reduce the pressure of other compression stages .g
    L 2 - 3:74
    20 I 25 26 I 53 56 52% 1 /
    53 56 52 55
    L-UCH S / TU,.
    fwz.
    85
    18
    83
    39
    SG s
    -L-1 S84
    .2
    3 53 56 52%
    53 56 52 55
    L-UCH S / TU,.
    86
    thirty
    fte.3
    t.S
    类似技术:
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    同族专利:
    公开号 | 公开日
    OA07764A|1985-08-30|
    DE3462945D1|1987-05-07|
    AU2746084A|1984-11-08|
    US4539028A|1985-09-03|
    FR2545589A1|1984-11-09|
    JPS6099982A|1985-06-03|
    NO841803L|1984-11-07|
    EP0125980B1|1987-04-01|
    NO159683C|1989-01-25|
    JPH0627618B2|1994-04-13|
    ES532222A0|1985-01-01|
    EP0125980A2|1984-11-21|
    ES8502536A1|1985-01-01|
    NO159683B|1988-10-17|
    EP0125980A3|1984-12-27|
    CA1226206A|1987-09-01|
    FR2545589B1|1985-08-30|
    IN161272B|1987-11-07|
    AU560904B2|1987-04-16|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR8307620A|FR2545589B1|1983-05-06|1983-05-06|METHOD AND APPARATUS FOR COOLING AND LIQUEFACTING AT LEAST ONE GAS WITH LOW BOILING POINT, SUCH AS NATURAL GAS|
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