Patent Application
20170356687
The present invention relates to a gas liquefaction apparatus and a gas liquefaction method in which, for example, natural gas is liquefied as liquefied natural gas.
A process of liquefying, for example, natural gas (NG) as liquefied natural gas (LNG) employs a so-called “closed loop type” in which a refrigerant having a specific composition (for example, nitrogen (N2) and a mixed refrigerant) is used and the refrigerant for exclusive use is circulated as a closed system. Therefore, there are following issues as the small- and mid-sized liquefaction process of natural gas in which a simple apparatus is desired.
1) A refrigerant manufacturing facility and a storage facility are required, or when the refrigerant is not manufactured, it is required to purchase the refrigerant.
2) When a mixed refrigerant is used as the refrigerant in the closed loop type, if a feed composition changes, the refrigerant composition needs to be adjusted, which is troublesome. Further, because mixing of the refrigerants needs to be performed accurately, time is required for the startup and the plant stability. Therefore, if shut-down and restart are repeated frequently, this process is not suitable.
3) When nitrogen (N2) is used as the refrigerant in the closed loop type, it is generally required to boost the nitrogen refrigerant pressure to a high pressure equal to or higher than 80 kg/cm2. Therefore, facilities such as a compressor and supply facilities such as piping and valves become expensive.
Therefore, in recent years, a technique of an open loop cycle process in which the natural gas is directly used as the refrigerant has been proposed (Patent Literature 1).
Patent Literature 1: Japanese Patent Application National Publication No. 2010-537151
However, according to the proposal described in Patent Literature 1, a plurality of cooling loops are required in a heat exchange area, and heat exchange facilities become complicated. Therefore, emergence of a technique that realizes further facility cost reduction and power reduction has been desired.
One or more embodiments of the present invention provide a gas liquefaction apparatus and a gas liquefaction method in which the heat exchange facilities are simple and facility cost reduction and power reduction are realized.
The first aspect of the present disclosure includes a gas liquefaction apparatus. The gas liquefaction apparatus includes: a source-gas supply line for supplying source gas; a room-temperature heat exchanger, a preliminary-cooling heat exchanger, and a liquefaction/supercooling heat exchanger that are provided in series sequentially in the source-gas supply line to cool the source gas; a separation drum that separates the source gas containing a condensate, which has been cooled by heat exchange up to a liquefaction temperature of the source gas or below, into a gas component and a liquefied component; a refrigerant-gas supply line that uses a gas component separated by the separation drum as refrigerant gas to supply the refrigerant gas in a direction opposite to a supply direction of the source gas, in order of the liquefaction/supercooling heat exchanger, the preliminary-cooling heat exchanger, and the room-temperature heat exchanger, thereby cooling the source gas; a compressor provided at an end portion of the refrigerant-gas supply line to compress the refrigerant gas used for cooling; a compressed-gas extraction line for extracting compressed gas compressed by the compressor from the compressor; a mixing unit that mixes the compressed gas with the source gas by connecting an end of the compressed-gas extraction line to the source-gas supply line at an upstream side of the room-temperature heat exchanger; an extraction line branched from the source-gas supply line at either one of or both of a position between the room-temperature heat exchanger and the preliminary-cooling heat exchanger or a position between the preliminary-cooling heat exchanger and the liquefaction/supercooling heat exchanger to extract a part of the source gas heat-exchanged; an expansion turbine connected with an end of the extraction line to adiabatically expand a part of the source gas extracted; and a cooling source-gas supply line for supplying cooling source gas temperature-dropped in the expansion turbine to the refrigerant-gas supply line at an upstream side of the liquefaction/supercooling heat exchanger.
The second aspect of the present disclosure includes a gas liquefaction apparatus. The gas liquefaction apparatus includes: a source-gas supply line for supplying source gas; a room-temperature heat exchanger, a preliminary-cooling heat exchanger, and a liquefaction/supercooling heat exchanger that are provided in series sequentially in the source-gas supply line to cool the source gas by heat exchange with refrigerant gas; a separation drum provided at an end portion of the source-gas supply line to separate cooled source gas containing a condensate into a gas component and a liquefied component; a refrigerant-gas supply line that uses the gas component separated by the separation drum and cooled as refrigerant gas to supply the refrigerant gas in a direction opposite to a supply direction of the source gas, in order of the liquefaction/supercooling heat exchanger, the preliminary-cooling heat exchanger, and the room-temperature heat exchanger, to cool the source gas; a compressor provided at an end portion of the refrigerant-gas supply line to compress the refrigerant gas; a compressed-gas extraction line for extracting compressed gas compressed by the compressor; a mixing unit that mixes the compressed gas with the source gas by connecting an end of the compressed-gas extraction line to the source-gas supply line on an upstream side of the room-temperature heat exchanger; a first extraction line branched from the source-gas supply line between the room-temperature heat exchanger and the preliminary-cooling heat exchanger to extract a part of the source gas heat-exchanged in the room-temperature heat exchanger; a warm expansion turbine connected with an end of the first extraction line to adiabatically expand a part of the source gas extracted; a first cooling-source-gas supply line for supplying first cooling source gas temperature-dropped in the warm expansion turbine to the refrigerant-gas supply line between the preliminary-cooling heat exchanger and the liquefaction/supercooling heat exchanger; a second extraction line branched from the source-gas supply line between the preliminary-cooling heat exchanger and the liquefaction/supercooling heat exchanger to extract a part of the source gas heat-exchanged in the preliminary-cooling heat exchanger; a cold expansion turbine connected with an end of the second extraction line to adiabatically expand a part of the source gas extracted; and a second cooling-source-gas supply line for supplying second cooling source gas temperature-dropped in the cold expansion turbine to the refrigerant-gas supply line between the liquefaction/supercooling heat exchanger and the separation drum.
The third aspect of the present disclosure includes the gas liquefaction apparatus in the second aspect. In the gas liquefaction apparatus, the liquefaction/supercooling heat exchanger is divided into two heat exchangers to form a liquefaction heat exchanger and a supercooling heat exchanger, and the liquefaction heat exchanger and the supercooling heat exchanger are provided in series, and the first cooling source gas temperature-dropped in the warm expansion turbine is branched into two parts, and branched first cooling source gas is respectively supplied to a refrigerant-gas supply line between the preliminary-cooling heat exchanger and the liquefaction heat exchanger, and that between the liquefaction heat exchanger and the supercooling heat exchanger.
The fourth aspect of the present disclosure includes the gas liquefaction apparatus in any one of the first to third aspect. In the gas liquefaction apparatus, a cooler that cools the source gas is provided in the source-gas supply line at an upstream side of the room-temperature heat exchanger.
The fifth aspect of the present disclosure includes the gas Liquefaction apparatus in any one of the first to fourth aspect. In the gas liquefaction apparatus, a heavy component separator that separates a heavy component from an extraction liquid acquired by extracting a part of the source gas is provided.
The sixth aspect of the present disclosure includes the gas liquefaction apparatus in any one of the first to fifth aspect. In the gas liquefaction apparatus, a boil-off gas supply line for supplying boil-off gas is provided on an upstream side of the compressor connected to the refrigerant-gas supply line.
The seventh aspect of the present disclosure includes a gas liquefaction method of an open loop cycle process in which source gas is cooled up to a liquefaction temperature to manufacture a gas liquefied substance from a cooled gas component and a liquefied component. The gas liquefaction apparatus includes: a heat-exchange step of heat-exchanging the cooled gas component as refrigerant gas in at least two heat exchanging units, while supplying the refrigerant gas in a direction opposite to a supply direction of the source gas; an adiabatic expansion step of extracting a part of cooled source gas between the heat exchanging units and adiabatically expanding the part of the source gas; and a refrigerant-gas supply step of supplying cooling source gas temperature-dropped at the adiabatic expansion step to the refrigerant gas.
According to one or more embodiments of the present invention, a part of the heat-exchanged source gas is extracted at either one of or both of a position between the room-temperature heat exchanger and the preliminary-cooling heat exchanger or a position between the preliminary-cooling heat exchanger and the liquefaction/supercooling heat exchanger, and is adiabatically expanded in the expansion turbine, thereby acquiring the temperature-dropped cooling source gas. The acquired cooling source gas is joined with the refrigerant gas to acquire a sufficient cooling amount for sequentially cooling the source gas in the respective heat exchangers. Accordingly, the heat exchange facilities have a simple configuration, thereby enabling to reduce the facility cost and power.
Embodiments of the present invention will be described in detail below with reference to the accompanying drawings. The present invention is not limited to the embodiments, and there are a plurality of embodiments, combinations thereof are also included in the present invention.
According to the present embodiment, for example, natural gas (NG) containing methane as a main component is used as the source gas 11, which is liquefied to become liquefied natural gas (LNG). The pressure of the natural gas is, for example, about 30 kg/cm2 to 70 kg/cm2 supplied by a pipeline. Other than the natural gas, it can be applied in a case when air is to be liquefied, for example.
According to the present embodiment, the source-gas supply line L1 forms a liquefaction line of a supply gas stream for supplying the source gas 11, and the refrigerant-gas supply line L2 forms a cooling line of a refrigerant gas stream for supplying the refrigerant gas 21. At a position where heat exchange is performed between these two lines, the room-temperature heat exchanger 12, the preliminary-cooling heat exchanger 13, and the liquefaction/supercooling heat exchanger 14 are provided sequentially as heat exchange units. The source gas 11 supplied by the source-gas supply line L1 is indirectly cooled in the heat exchanging units 12a, 13a, and 14a by the refrigerant gas 21 supplied in an opposite direction by the refrigerant-gas supply line L2. At this time, an open loop cycle process in which the unliquefied gas component of the source gas 11 is utilized as the refrigerant gas 21 is realized in an end zone of the liquefaction line.
According to the present embodiment, as the heat exchanging units 12a, 13a, and 14a respectively installed inside the room-temperature heat exchanger 12, the preliminary-cooling heat exchanger 13, and the liquefaction/supercooling heat exchanger 14, for example, a plate-fin type heat exchanger is used. However, the heat exchanging unit is not limited thereto, so long as it is a unit that efficiently performs heat exchange of the source gas 11 by using the refrigerant gas 21.
The room-temperature heat exchanger 12 performs heat exchange of the source gas 11 at a room temperature (for example, 20° C. to 40° C.) by the refrigerant gas 21, for example, to about 0° C. or 0° C. or below.
The preliminary-cooling heat exchanger 13 performs heat exchange of the source gas 11 cooled to near 0° C. by the refrigerant gas 21, for example, to −80° C. or below.
The liquefaction/supercooling heat exchanger 14 performs heat exchange of the source gas 11 cooled to −80° C. or below by the refrigerant gas 21, for example, to −120° C. or below. The cooling temperature in the respective heat exchangers is a rough indication, and appropriately changed according to the composition of the source gas 11 and conditions of the refrigerant gas 21.
The source gas 11 cooled in the liquefaction/supercooling heat exchanger 14 is expanded by an expansion valve 51 interposed between the liquefaction/supercooling heat exchanger 14 and the separation drum 15 and then introduced into the separation drum 15 connected to the end side of the source-gas supply line L1. In the separation drum 15, the source gas 11 is separated into a gas component of flash gas and a liquefied component of the liquefied natural gas.
Because the flash gas has been cooled, the flash gas is introduced into the refrigerant-gas supply line L2 as the refrigerant gas 21 in order of the liquefaction/supercooling heat exchanger 14, the preliminary-cooling heat exchanger 13, and the room-temperature heat exchanger 12. The flash gas is then used circularly as the refrigerant gas for cooling the source gas 11 in the respective heat exchanging units 14a, 13a, and 12a.
The refrigerant gas 21 used for cooling the source gas 11 is introduced into the compressor 31 provided at the end portion of the refrigerant-gas supply line L2. The compressor 31 is a two-stage compressor in the present embodiment, but is not limited thereto, and can be installed in a plurality of stages more than two. The refrigerant gas 21 is compressed to a predetermined pressure (to the same level as the source gas) by the compressor 31, mixed with the source gas 11 again in the mixing unit 32, and recirculated.
The liquefied natural gas (LNG) of the liquefied component separated by the separation drum 15 is separately collected as a product.
According to the present embodiment, the part 11a of the source gas 11 heat-exchanged in the preliminary-cooling heat exchanger 13 provided in the source-gas supply line L1 is extracted by the extraction line L4, and adiabatically expanded by the expansion turbine 33 connected to the end of the extraction line L4. Thereby the cooling source gas 34 temperature-dropped, for example, to −150° C. or below can be acquired.
The acquired cooling source gas 34 is joined with the refrigerant gas 21 at a refrigerant joining portion 41 provided in the refrigerant-gas supply line L2 between the liquefaction/supercooling heat exchanger 14 and the separation drum 15 on the upstream side of the liquefaction/supercooling heat exchanger 14 via the cooling source-gas supply line L5. By joining the cooling source gas 34 with the refrigerant gas 21 in the refrigerant joining portion 41, the refrigerant for a heat exchange capacity required for cooling in the liquefaction/supercooling heat exchanger 14, the preliminary-cooling heat exchanger 13, and the room-temperature heat exchanger 12 is supplied.
Therefore, the extraction amount to be extracted of the part 11a of the source gas 11 heat-exchanged by the preliminary-cooling heat exchanger 13 is adjusted by an adjustment unit (not illustrated) or in advance, so as to acquire a heat capacity for cooling the source gas 11 to a predetermined temperature by the cooling source gas 34 acquired by the expansion turbine 33.
An operation of the gas liquefaction apparatus 10A according to the present embodiment is described with reference to
The source gas 11 cooled and liquefied sequentially by the refrigerant gas 21 in the room-temperature heat exchanger 12, the preliminary-cooling heat exchanger 13, and the liquefaction/supercooling heat exchanger 14 is expanded by the expansion valve 51 installed in front of the separation drum 15 provided in the end zone at the end of the source-gas supply line L1, and then separated into a gas component and a liquefied component. The liquefied component is delivered, for example, to a storage tank or a pipeline as liquefied natural gas (LNG).
Because the gas component separated by the separation drum has been cooled, the gas component is delivered to the refrigerant-gas supply line L2 from a top portion of the separation drum 15 as the refrigerant gas 21, to form a refrigerant gas stream. The refrigerant gas 21 flows in a direction opposite to the supply direction of the source gas 11 from the liquefaction/supercooling heat exchanger 14, the preliminary-cooling heat exchanger 13, and the room-temperature heat exchanger 12, to cool the source gas 11 indirectly in the respective heat exchanging units 14a, 13a, and 12a. By the heat exchange and cooling by the refrigerant gas 21, the liquefied component of the source gas 11 is separated as liquefied natural gas (LNG), and the unliquefied gas component that has not been liquefied is used for cooling as the refrigerant gas 21. After having contributed to cooling, the refrigerant gas 21 is delivered to the compressor 31 provided in the end zone at the end of the refrigerant-gas supply line L2 and compressed to the same level as the gas pressure of the source gas 11. The compressed gas 22 that has been compressed is mixed with the source gas 11 in the mixing unit 32, and is supplied again as the source gas 11. Accordingly, the open loop cycle process is constructed in which the unliquefied gas of the source gas 11 is used as the refrigerant gas 21, and is mixed with the source gas 11 again and liquefied, and circulated and reused.
According to the present embodiment, the part 11a of the source gas 11 cooled in the preliminary-cooling heat exchanger 13 provided in the source-gas supply line L1 is extracted by the extraction line L4, and adiabatically expanded by the expansion turbine 33 connected to the end of the extraction line L4, thereby acquiring the cooling source gas 34 temperature-dropped, for example, to −150° C. or below.
The acquired cooling source gas 34 is joined with the refrigerant gas 21 in the refrigerant joining portion 41 provided in the refrigerant-gas supply line L2 between the liquefaction/supercooling heat exchanger 14 and the separation drum 15 on the upstream side of the liquefaction/supercooling heat exchanger 14 via the cooling source-gas supply line L5. Due to this joining, the cooling source gas 34 is supplied to the refrigerant gas 21, so that a heat exchange amount required for cooling in the liquefaction/supercooling heat exchanger 14, the preliminary-cooling heat exchanger 13, and the room-temperature heat exchanger 12 is supplied.
In this manner, only the refrigerant gas 21 separated by the separation drum 15 cannot cool the source gas 11 sufficiently. Therefore, the part 11a of the source gas 11 heat-exchanged in the preliminary-cooling heat exchanger 13 is extracted, and introduced into the expansion turbine 33 to be adiabatically expanded, thereby acquiring the cooling source gas 34. The cooling source gas 34 is joined with the refrigerant gas 21 in the refrigerant joining portion 41 in the refrigerant-gas supply line L2, thereby enabling to acquire the refrigerant gas 21 having the cooling amount sufficient for cooling the source gas 11 sequentially in the respective heat exchanging units 14a, 13a, and 12a.
Further, the power of the compressor 31 is collected by the power of the expansion turbine 33 connected coaxially to enable reduction of the compression power. Coolers 31a and 31b are provided in the compressor 31 to cool the compressed gas.
According to the present embodiment, the heat exchanging facility has a simple configuration such that the source-gas stream line and the refrigerant-gas stream line are provided in the direction opposite to each other to perform heat exchange sequentially in the heat exchanging units 12a, 13a, and 14a of the room-temperature heat exchanger 12, the preliminary-cooling heat exchanger 13, and the liquefaction/supercooling heat exchanger 14. Accordingly, a complicated heat exchange loop is not required, and facility cost reduction and power reduction can be realized.
A gas liquefaction method according to one or more embodiments of the present invention is a gas liquefaction manufacturing method of an open loop cycle process in which the source gas (for example, natural gas) 11 is cooled up to a liquefaction temperature to manufacture liquefied natural gas (LNG) of a gas liquefied substance from the cooled gas component and the liquefied component. The gas liquefaction method includes a heat-exchange step of heat-exchanging the cooled gas component as the refrigerant gas 21 in at least two heat exchanging units (in the present embodiment, three heat exchanging units 14a, 13a, 12a), while supplying the refrigerant gas 21 in the direction opposite to the supply direction of the source gas 11, an adiabatic expansion step of extracting the part 11a of the source gas 11 after being cooled in the heat exchanging unit 13a of the preliminary-cooling heat exchanger 13, for example, between the heat exchanging unit 13a of the preliminary-cooling heat exchanger 13 and the heat exchanging unit 14a of the liquefaction/supercooling heat exchanger 14 and adiabatically expanding the part 11a of the source gas 11 by the expansion turbine 33, and a refrigerant-gas supply step of supplying the cooling source gas 34 temperature-dropped at the adiabatic expansion step to the refrigerant gas 21.
According to the present embodiment, the extraction line L4 branched from the source-gas supply line L1 between the preliminary-cooling heat exchanger 13 and the liquefaction/supercooling heat exchanger 14 to extract the part 11a of the source gas 11 heat-exchanged in the preliminary-cooling heat exchanger 13 is provided. However, the present invention is not limited thereto. For example, an extraction line L4 for extracting the part 11a of the source gas 11 heat-exchanged in the room-temperature heat exchanger 12 from a position between the room-temperature heat exchanger 12 and the preliminary-cooling heat exchanger 13 provided in the source-gas supply line L1 can be provided. Thereby the part 11a of the source gas 11 is delivered to the expansion turbine 33 to be adiabatically expanded in the expansion turbine 33, to acquire the temperature-dropped cooling source gas 34. The acquired cooling source gas 34 can be joined with the refrigerant gas 21 in the refrigerant joining portion 41, to supply a refrigerant body having a sufficient cooling capacity.
A gas liquefaction apparatus according to a second embodiment of the present invention is described with reference to the drawings.
In the present embodiment, the first cooling source gas 34A acquired in the warm expansion turbine 33A is joined with the refrigerant gas 21 at the first refrigerant joining portion 41A provided in the refrigerant-gas supply line L2 between the preliminary-cooling heat exchanger 13 and the liquefaction/supercooling heat exchanger 14, via the first cooling-source-gas supply line L5A.
The second cooling source gas 34B acquired in the cold expansion turbine 33B is joined with the refrigerant gas 21 at the second refrigerant joining portion 41B provided in the refrigerant-gas supply line L2 between the liquefaction/supercooling heat exchanger 14 and the separation drum 15, via the second cooling-source-gas supply line L5B.
By joining the first cooling source gas 34A and the second cooling source gas 34B with the refrigerant gas 21 sequentially in the first and second refrigerant joining portions 41A and 41B, the refrigerant having the heat exchange capacity required for cooling in the liquefaction/supercooling heat exchanger 14, the preliminary-cooling heat exchanger 13, and the room-temperature heat exchanger 12 is supplied.
A test for confirming the effects of the second embodiment of the present invention was performed.
As illustrated in
In the room-temperature heat exchanger 12, the source gas 11 is cooled up to 0° C. by the refrigerant gas 21 at −34.4° C. flowing in the refrigerant-gas supply line L2. A part 11a of the source gas 11 at 0° C. is delivered to the warm expansion turbine 33A, where the part 11a of the source gas 11 becomes the first cooling source gas 34A at −131.1° C. The first cooling source gas 34A is joined with the refrigerant gas 21 in the first refrigerant joining portion 41A and then mixed with the refrigerant gas 21 at −153.1° C. flowing in the refrigerant-gas supply line L2 to become the refrigerant gas 21 at −145.8° C. and is introduced into the preliminary-cooling heat exchanger 13.
In the preliminary-cooling heat exchanger 13, the source gas 11 is cooled by the refrigerant gas 21 at −145.8° C. flowing in the refrigerant-gas supply line L2, and cooled from 0° C. to −88.2° C. The part 11b of the source gas 11 at −88.2° C. is delivered to the cold expansion turbine 33B, where the part 11b of the source gas 11 becomes the second cooling source gas 34B at −155.2° C. The second cooling source gas 34B is joined with the refrigerant gas 21 in the second refrigerant joining portion 41B and then mixed with the refrigerant gas 21 at −154.1° C. flowing in the refrigerant-gas supply line L2 to become the refrigerant gas 21 at −155.2° C. and is introduced into the liquefaction/supercooling heat exchanger 14.
In the liquefaction/supercooling heat exchanger 14, the source gas 11 is cooled by the refrigerant gas 21 at −155.2° C. flowing in the refrigerant-gas supply line L2, to be cooled from −88.2° C. to −127.0° C.
The source gas 11 cooled to −127.0° C. is expanded by the expansion valve 51 installed in front of the separation drum 15, and is separated by a flash action in the separation drum 15 into the gas component and the liquefied component at −154.1° C. The liquefied component is delivered to the storage tank or the pipeline as liquefied natural gas (LNG). The gas component is delivered to the refrigerant-gas supply line L2 as the refrigerant gas 21 and is circulated and used.
The refrigerant gas 21 contributes to cooling, and then becomes gas having a temperature of 19.1° C. and a pressure of 1.2 kg/cm2A, and is delivered to the compressor 31 provided in the end zone at the end of the refrigerant-gas supply line L2. In the compressor 31, the refrigerant gas 21 is compressed to the same level of a gas pressure of the source gas 11, that is, a temperature of 40° C. and a pressure of 40.0 kg/cm2A, and joined with the source gas 11 in the mixing unit 32 and liquefied again.
A gas liquefaction apparatus according to a third embodiment of the present invention is described with reference to the drawings.
Further, on a front side of the compressor 31 between the room-temperature heat exchanger 12 and the compressor 31 in the refrigerant-gas supply line L2, a boil-off gas supply line L11 is connected to supply boil-off gas (BOG) partially gasified by natural heat input, for example, in the LNG facilities from outside. By supplying the BOG via the boil-off gas supply line L11 and joining the BOG with the refrigerant gas 21 after having contributed to cooling, the BOG can be effectively re-liquefied. Accordingly, a re-liquefaction facility only for the BOG is not required.
Further, in the present embodiment, a heavy-component separating unit 53a is provided in the first extraction line L4A for extracting the part 11a of the source gas 11 cooled by the room-temperature heat exchanger 12, to separate a heavy component liquid generated at the time of being cooled in the room-temperature heat exchanger 12. Further, in the present embodiment, a heavy-component separating unit 53b is provided in the second extraction line L4B for extracting the part 11b of the source gas 11 cooled by the preliminary-cooling heat exchanger 13, to separate a heavy component liquid generated at the time of being cooled in the preliminary-cooling heat exchanger 13. If any liquid is not generated under the cooling conditions in the preliminary-cooling heat exchanger 13, installation of the heavy-component separating unit 53b may be unnecessary. Accordingly, by removing the heavy component, solidification in the heat exchanger on a wake side is prevented. The separated heavy component 54 is used, for example, as a fuel for driving the turbine.
Further, according to the present embodiment, by providing a liquid expander 55 including a liquefaction expansion turbine 55a and a pressure regulation valve 55b instead of the expansion valve 51 for expansion provided in front of the separation drum 15, consumed energy in the liquefaction process can be collected as electric energy.
A gas liquefaction apparatus according to a fourth embodiment of the present invention is described with reference to the drawings.
In the present embodiment, by using the geared compander 61, the efficiency of the compressor is improved even more as compared to the second embodiment.
A gas liquefaction apparatus according to a fifth embodiment of the present invention will be described with reference to the drawings.
The two separation drums 15 are provided, such that a first separation drum 15A and a second separation drum 15B having a different operating pressure are installed.
The refrigerant gas 21 separated by the first separation drum 15A flows in the refrigerant-gas supply line L2 at a pressure higher than the atmospheric pressure, and is heat-exchanged in the respective heat exchanging units 14b, 14a, 13a, and 12a of the supercooling heat exchanger 14B, the liquefaction heat exchanger 14A, the preliminary-cooling heat exchanger 13, and the room-temperature heat exchanger 12, and introduced into the side of the compressor 31. Accordingly, the power in the compressor 31 is reduced because the pressure is not released up to the atmospheric pressure as in the first embodiment.
Further, because the second cooling source gas 34B temperature-dropped by the cold expansion turbine 33B has a mixed phase of the gas component and the liquefied component, the second cooling-source-gas supply line L5B is connected to the first separation drum 15A. The second cooling source gas 34B is directly introduced into the first separation drum 15A and flashed therein to separate the gas component and the liquefied component from each other.
The liquefied component separated in the first separation drum 15A is expanded by the expansion valve 51B installed in front of the second separation drum 15B and flashed in the second separation drum 15B, thereby being separated into the gas component and the liquefied component. The liquefied component is delivered to the storage tank or the pipeline as liquefied natural gas (LNG). The gas component is separately used as fuel gas.
A test for confirming the effects of the fifth embodiment of the present invention was performed.
As illustrated in
In the room-temperature heat exchanger 12, the source gas 11 is cooled by the refrigerant gas 21 at −26.3° C. flowing in the refrigerant-gas supply line L2 and cooled up to −5.0° C. A part 11a of the source gas 11 at −5.0° C. is delivered to the warm expansion turbine 33A, where the part 11a of the source gas 11 becomes first cooling source gas 34A-1 and first cooling source gas 34A-2 at −112.7° C. The cooling source gas 34A-1 is joined with the refrigerant gas 21 at −91.4° C. flowing in the refrigerant-gas supply line L2 after having been cooled in the liquefaction heat exchanger 14A, at the first refrigerant joining portion 41A-1 to become the refrigerant gas 21 at −95.0° C. and is introduced into the preliminary-cooling heat exchanger 13.
Further, the first cooling source gas 34A-2 at −112.7° C. is joined with the refrigerant gas 21 at −91.4° C. flowing in the refrigerant-gas supply line L2 after having been cooled in the supercooling heat exchanger 14B at the second refrigerant joining portion 41A-2 to become the refrigerant gas 21 at −104.8° C. and is introduced into the liquefaction heat exchanger 14A.
In the preliminary-cooling heat exchanger 13, the source gas 11 is cooled by the refrigerant gas 21 at −95.0° C. flowing in the refrigerant-gas supply line L2, to be cooled from −5.0° C. to −88.4° C. The part 11b of the source gas 11 at −88.4° C. is delivered to the cold expansion turbine 33B, where the part 11b of the source gas 11 becomes the second cooling source gas 34B at −144.3° C. The second cooling source gas 34B is introduced into the first separation drum 15A and flashed to become the refrigerant gas 21 at −144.3° C. and is introduced into the refrigerant-gas supply line L2 and then into the supercooling heat exchanger 14B.
In the supercooling heat exchanger 14B, the source gas 11 is cooled by the refrigerant gas 21 at −144.3° C. flowing in the refrigerant-gas supply line L2, and thus the source gas 11 is cooled from −88.4° C. to −141.0° C.
The source gas 11 cooled to −141.0° C. is expanded by the expansion valve 51A installed in front of the first separation drum 15A, and is then separated by the first separation drum 15A into the gas component and the liquefied component at −144.3° C. and 3.5 kg/cm2A. The liquefied component is expanded by the expansion valve 51B installed in front of the second separation drum 15B, and is then separated by the second separation drum 15B into the gas component and the liquefied component at −161.3° C. and 1.05 kg/cm2A.
The liquefied component is delivered, for example, to the storage tank or the pipeline as liquefied natural gas (LNG). The gas component is used as fuel gas.
The refrigerant gas 21 contributes to cooling, and then becomes gas having a temperature of 36.3° C. and a pressure of 3.0 kg/cm2A, and is delivered to the compressor 31 provided in the end zone at the end of the refrigerant-gas supply line L2, where the refrigerant gas 21 is compressed to the same level of the gas pressure of the source gas 11, that is, a temperature of 40° C. and a pressure of 40.0 kg/cm2A, and mixed with the source gas 11 in the mixing unit 32 and liquefied again. At the time of re-liquefaction, because the refrigerant gas has a higher pressure than that of test example 1, the compression load of the compressor can be reduced, thereby enabling to reduce the power.
As a result, in the present test example 2, significant improvement can be realized in a basic unit in manufacturing as compared to the test example 1.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2015-003546 | Jan 2015 | JP | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/JP2016/050019 | 1/4/2016 | WO | 00 |
