WO2017115723A1 - Intermediate medium carburetor - Google Patents

Abstract

An intermediate medium carburetor 10 is equipped with: an intermediate medium evaporator E1 which evaporates at least part of a liquid intermediate medium M through heat exchange between seawater and the intermediate medium M; and an LNG evaporator E2 which condenses the intermediate medium M evaporated by the intermediate medium evaporator E1 in order to vaporize LNG into natural gas (NG) and causes the NG to flow out. The LNG evaporator E2 is configured from a laminated heat exchanger having a laminated body which is formed with first flow paths that are paths for the flow of the intermediate medium M and second flow paths that are paths for the flow of the LNG. The laminated heat exchanger is installed in an orientation where the first flow paths extend in the vertical direction or in a direction inclined to the vertical direction so that the intermediate medium M flows down in the first flow paths due to gravity .

Description

Intermediate medium vaporizer

The present invention relates to an intermediate medium type vaporizer.

Conventionally, as disclosed in Patent Document 1 below, an intermediate medium type vaporizer that uses an intermediate medium in addition to a heat source fluid is known as an apparatus for vaporizing a low temperature liquid such as LNG. As shown in FIG. 10, the intermediate medium type vaporizer disclosed in Patent Document 1 includes an intermediate medium evaporator 81, an LNG evaporator 82, and a warmer 83. Further, the intermediate medium type vaporizer is provided with an inlet chamber 85, a large number of heat transfer tubes 86, an intermediate chamber 87, a large number of heat transfer tubes 88 and an outlet chamber 89 in this order as a path through which seawater as a heat source fluid passes. It has been. The heat transfer tube 86 is disposed in the heater 83, and the heat transfer tube 88 is disposed in the intermediate medium evaporator 81. An intermediate medium (for example, propane) having a boiling point lower than that of seawater is accommodated in the intermediate medium evaporator 81.

The LNG evaporator 82 includes an inlet chamber 91 and an outlet chamber 92, and a large number of heat transfer tubes 93 communicating with both the chambers 91 and 92. Each heat transfer tube 93 is substantially U-shaped and protrudes to the upper part in the intermediate medium evaporator 81. The outlet chamber 92 communicates with the warmer 83 via the NG conduit 94.

In such a vaporizer, seawater, which is a heat source fluid, reaches the outlet chamber 89 through the inlet chamber 85, the heat transfer tube 86, the intermediate chamber 87 and the heat transfer tube 88. At this time, the seawater passing through the heat transfer pipe 88 exchanges heat with the liquid intermediate medium M in the intermediate medium evaporator 81 to evaporate the intermediate medium M.

On the other hand, LNG to be vaporized is introduced into the heat transfer tube 93 from the inlet chamber 91. The heat exchange between the LNG in the heat transfer tube 93 and the evaporation intermediate medium in the intermediate medium evaporator 81 causes the intermediate medium M to condense, and the LNG evaporates in the heat transfer tube 93 by receiving the heat of condensation. It becomes. This NG is introduced into the heater 83 from the outlet chamber 92 through the NG conduit 94, further heated by heat exchange with seawater flowing through the heat transfer pipe 86 in the heater 83, and then supplied to the use side. The

In the intermediate medium vaporizer disclosed in Patent Document 1, the LNG evaporator 82 has a large number of heat transfer tubes 93. For this reason, the LNG evaporator 82 becomes a considerable weight.

JP 2000-227200 A

An object of the present invention is to reduce the weight of the intermediate medium type vaporizer.

An intermediate medium vaporizer according to one aspect of the present invention includes an intermediate medium evaporation unit that evaporates at least a part of the intermediate medium by heat exchange between a heat source medium and a liquid intermediate medium, and the intermediate medium evaporation unit. And a liquefied gas vaporization section that vaporizes the low-temperature liquefied gas and causes the gas to flow out by condensing the evaporated intermediate medium, and the liquefied gas vaporization section has a first flow path that is a flow path of the intermediate medium. The laminated heat exchanger includes a laminated heat exchanger having a laminate in which a first channel layer and a second channel layer having a second channel that is a channel for low-temperature liquefied gas are laminated. The first flow path is installed in a posture extending in a vertical direction or a direction inclined with respect to the vertical direction so that the intermediate medium flows down by gravity in the first flow path.

It is a figure which shows roughly the structure of the intermediate medium type vaporizer | carburetor which concerns on 1st Embodiment of this invention. It is a figure which shows roughly the structure of the LNG evaporator provided in the said intermediate | middle medium type vaporizer. It is a figure which shows roughly the structure of the laminated heat exchanger which comprises the warmer provided in the said intermediate | middle medium type vaporizer. It is a figure which shows roughly the structure of the intermediate | middle medium type vaporizer | carburetor which concerns on the modification of 1st Embodiment of this invention. It is a figure which shows roughly the structure of the intermediate | middle medium type vaporizer | carburetor which concerns on the modification of 1st Embodiment of this invention. It is a figure which shows roughly the structure of the intermediate | middle medium type vaporizer | carburetor which concerns on the modification of 1st Embodiment of this invention. It is a figure which shows roughly the structure of the intermediate | middle medium type vaporizer | carburetor which concerns on the modification of 1st Embodiment of this invention. It is a figure which shows roughly the structure of the intermediate-medium vaporizer | carburetor which concerns on 2nd Embodiment of this invention. It is a figure which shows schematically the structure of the intermediate | middle medium type vaporizer | carburetor which concerns on the modification of 2nd Embodiment of this invention. It is a figure which shows roughly the structure of the conventional intermediate | middle medium type vaporizer | carburetor.

Hereinafter, embodiments for carrying out the present invention will be described in detail with reference to the drawings.

(First embodiment)
As shown in FIG. 1, an intermediate medium vaporizer (hereinafter simply referred to as a vaporizer) 10 according to the first embodiment is a low-temperature liquefied gas that heats seawater, which is a heat source medium, via an intermediate medium M. It is a device that obtains NG (natural gas) by transmitting to LNG (liquefied natural gas) and vaporizing LNG. As the intermediate medium M, for example, propane or the like can be used. The vaporizer 10 may be configured as a device that vaporizes or heats a low-temperature liquefied gas other than LNG, such as liquefied petroleum gas (LPG) or liquid nitrogen (LN ₂ ).

The vaporizer 10 includes an intermediate medium evaporator E1 that is an intermediate medium evaporator, an LNG evaporator E2 that is a liquefied gas vaporizer, and a heater E3. The LNG evaporator E2 is disposed in the shell 11 of the intermediate medium evaporator E1. The warmer E3 is disposed on the side of the shell 11. An intermediate chamber 14 is formed between the shell 11 and the heater E3.

The shell 11 has a shape that is long in the horizontal direction. A large number of heat transfer tubes 20 of the intermediate medium evaporator E1 are disposed in the lower part of the shell 11. In the upper part of the shell 11, an LNG evaporator E2 is disposed.

The intermediate chamber 14 is adjacent to one of the pair of side walls constituting the shell 11 of the intermediate medium evaporator E1, and the outlet chamber 18 is adjacent to the other. The heat transfer tube 20 is disposed in the lower part of the space in the shell 11. The heat transfer tube 20 includes a first side wall 11 a that functions as a partition wall between the intermediate chamber 14 and the shell 11, an outlet chamber 18, and a shell among a pair of side walls that constitute the shell 11 of the intermediate medium evaporator E 1. 11 and the second side wall 11b functioning as a partition wall with the inside. The heat transfer tube 20 has a shape extending linearly in one direction, but is not limited to this shape. The heat transfer tube 20 communicates with the intermediate chamber 14 and the outlet chamber 18.

A discharge pipe 24 for discharging seawater is connected to the outlet chamber 18. Seawater in the outlet chamber 18 is discharged to the outside through the discharge pipe 24.

In the shell 11, an intermediate medium (for example, propane) M having a boiling point lower than the temperature of seawater is accommodated. The intermediate medium M is accommodated to such an extent that the liquid level is positioned above all the heat transfer tubes (heat transfer tubes through which heat source fluid, for example, seawater flows) 20.

Above the outlet chamber 18, an LNG inlet chamber 26 and an outlet chamber 28 for leading out NG are provided. A supply pipe 30 for introducing LNG is connected to the inlet chamber 26. A lead-out pipe 32 for leading out NG is connected to the outlet chamber 28. In FIG. 1, the outlet chamber 28 is drawn for convenience so that the outlet chamber 28 is positioned above the inlet chamber 26, but in reality, the outlet chamber 28 and the inlet chamber 26 are a microchannel heat exchanger described later. It is arranged side by side according to the configuration. However, the configuration is not limited to this.

As shown in FIG. 2, the LNG evaporator E2 includes a micro-channel heat exchanger that is an example of a stacked heat exchanger having a stacked body 38 in which a first flow path 41a and a second flow path 42a are formed. Has been. Specifically, the microchannel heat exchanger has a configuration in which a laminated body 38 of flow path layers 41 and 42 made of a metal plate is sandwiched between end plates 43 and 43. The laminated body 38 includes a first flow path layer 41 in which a large number of flow paths (first flow paths) 41a through which the intermediate medium M flows and a large number of flow paths (second flow paths) 42a through which LNG flows. It has a configuration in which the recessed second flow path layers 42 are alternately stacked. Then, heat exchange is performed between the intermediate medium M flowing through each first flow path 41a and the LNG flowing through each second flow path 42a, and the LNG is vaporized by being heated.

The first flow path layer 41 and the second flow path layer 42 are both vertical and extend in a direction (horizontal direction) parallel to the direction in which the heat transfer tube 20 of the intermediate medium evaporator E1 extends. However, the flow path layers 41 and 42 are not limited to the vertical posture, and may be inclined. Moreover, the flow path layers 41 and 42 may be in a posture extending in a direction intersecting with this direction instead of being parallel to the direction in which the heat transfer tube 20 extends.

The first flow paths 41 a are formed so as to extend in the vertical direction, and are arranged in the longitudinal direction of the first flow path layer 41. No header is provided above the stacked body 38. Therefore, the upper end of the first flow path 41 a is opened in the shell 11. For this reason, the gaseous intermediate medium M in the shell 11 directly flows into the first flow path 41a without going through the header.

The first channel 41a is not limited to a configuration extending in a vertical direction, and may be formed in a shape extending in a direction inclined from the vertical direction. Moreover, the 1st flow path 41a is not restricted to the shape extended linearly, The structure which bends or meanders in the middle may be sufficient. In short, the first flow path 41a may be configured such that the intermediate medium M flows down from the inflow end to the outflow end by gravity in the first flow path 41a and flows out from the outflow end.

A liquid reservoir 45 is provided below the laminated body 38. The liquid reservoir 45 stores the intermediate medium M condensed in the first flow path 41 a and is directly coupled to the lower end portion of the stacked body 38. The liquid reservoir 45 is formed in a shape that covers the entire lower surface of the stacked body 38 so that the internal space thereof communicates with all the first flow paths 41a. That is, the liquid intermediate medium M is stored on the downstream side of the first flow path 41a. The lower part of the first flow path 41a is blocked by the liquid intermediate medium M stored in the liquid reservoir 45. There may be a gas layer between the liquid intermediate medium M collected at the lower end in the first flow path 41a and the liquid intermediate medium M collected in the liquid reservoir 45, or The gas layer may not exist. This will vary depending on the driving situation. In any state, since the liquid intermediate medium M is stored below the first flow path 41a, the gaseous intermediate medium M is sucked from the lower side of the first flow path 41a. It is prevented.

A liquid seal tube 46 is connected to the bottom surface of the liquid reservoir 45. The liquid seal tube 46 extends downward from the bottom surface of the liquid reservoir 45. The lower end portion of the liquid seal tube 46 is immersed in the intermediate medium M stored in the intermediate medium evaporator E1. More specifically, the lower end portion of the liquid seal tube 46 is immersed in the intermediate medium M and disposed above the heat transfer tubes 20 of the intermediate medium evaporator E1. That is, the liquid seal tube 46 connects the lower part of the LNG evaporator E2 and the upper part of the intermediate medium evaporator E1. Therefore, the bottom surface of the liquid reservoir 45 is disposed at a position away from the liquid surface of the intermediate medium M stored in the intermediate medium evaporator E1. For this reason, the LNG evaporator E2 is located above the liquid level of the intermediate medium evaporator E1.

The liquid reservoir 45 and the liquid seal tube 46 are filled with a liquid intermediate medium M. In other words, the liquid sealing tube 46 connects the liquid intermediate medium M in the liquid reservoir 45 and the liquid level of the liquid intermediate medium M accumulated in the intermediate medium evaporator E1. The liquid seal tube 46 has a cross-sectional area sufficiently smaller than the area of the bottom surface of the liquid reservoir 45.

Each of the second flow paths 42a is formed so as to extend in a direction orthogonal to the first flow path 41a, specifically, in the longitudinal direction of the second flow path layer 42, and is arranged so as to be lined up and down. . In addition, the 2nd flow path 42a is not restricted to the shape extended straightly, You may bend in the middle and may meander.

The flow paths 41a and 42a are formed, for example, by etching the metal plates 41 and 42, and have a semicircular cross-sectional groove shape, for example. The flow paths 41a and 42a have a flow path width of 0.2 mm to 3 mm, for example.

In the present embodiment, two sets of laminated bodies 38 of the flow path layers 41 and 42 sandwiched between the end plates 43 and 43 are provided. Then, in one set, LNG flows from the front of FIG. 2 toward the back, and in the other set, LNG after flowing through the one set flows from the back of FIG. 2 toward the front. That is, in this embodiment, it has a two-pass configuration. The liquid reservoir 45 is formed in a size communicating with the first flow path 41a of both paths. Instead of this configuration, the liquid reservoir 45 is replaced with the first liquid reservoir connected to the first flow path 41a in the stacked body 38 constituting the first path and the first reservoir in the stacked body 38 configuring the second path. It is good also as a structure provided separately with the 2nd liquid reservoir connected with 1 flow path 41a. In this case, the liquid seal tube 46 includes a first liquid seal tube connected to the first liquid reservoir and a second liquid seal tube connected to the second liquid reservoir.

2 are provided with headers on the back side and the near side in FIG. 2 (see FIG. 1). In FIG. 2, the front header (distribution header 48 and aggregate header 50) is omitted for convenience. The header flowed through the distribution header 48 (see FIG. 1) for distributing the LNG introduced through the inlet chamber 26 to the second flow paths 42a, and the second flow paths 42a in the first set of stacked bodies 38. The LNG is gathered, and the connection header 49 distributed to each second flow path 42a in the second set of stacked bodies 38 and the NG that flows through the second flow paths 42a in the second set of stacked bodies 38 are gathered. A collective header 50 (see FIG. 1) that leads to the outlet chamber 28 is provided. In FIG. 1, for the sake of convenience, the distribution header 48 and the collective header 50 are drawn so as to be lined up and down, but they are actually lined sideways.

In the present embodiment, the microchannel heat exchanger (LNG evaporator E2) has a configuration having two paths. However, the present invention is not limited to this, and the configuration has one path or three or more paths. Also good. Further, the stacked heat exchanger (LNG evaporator E2) is not limited to the case where it is constituted by a microchannel heat exchanger. For example, a large number of metal plates formed in a waveform may be stacked, and a space between adjacent metal plates may be configured by a plate fin heat exchanger formed as a first flow path and a second flow path. .

Return to Figure 1. A heater E <b> 3 is connected to the outlet pipe 32. The casing 52 of the heater E3 forms an intermediate chamber 14 between the shell 11 and the casing 52. On the side wall of the casing 52 opposite to the shell 11, for example, an inlet chamber 53 for seawater, which is a heat source medium, is provided. For example, seawater as a heat source medium is introduced into the inlet chamber 53.

In the housing 52, a large number of heat transfer tubes 54 (heat transfer tube heat exchanger E3b) through which, for example, seawater as a heat source medium circulates, and a stacked heat exchanger E3a into which NG is introduced from the outlet tube 32 are arranged. It is installed. Further, an intermediate medium M2 is enclosed in the casing 52 of the heater E3. The intermediate medium M2 is made of propane, for example. The heat transfer tube 54 is bridged between a side wall adjacent to the intermediate chamber 14 and a side wall adjacent to the inlet chamber 53. The heat transfer tube 54 is disposed below the liquid level of the liquid intermediate medium M2 stored in the casing 52, and the stacked heat exchanger E3a is disposed above the liquid level.

In the present embodiment, the stacked heat exchanger E3a of the warmer E3 is configured by a microchannel heat exchanger, and has the same configuration as the LNG evaporator E2. Therefore, as shown in FIG. 3, the stacked heat exchanger E3a in the heater E3 also includes the first flow path layer 56 in which the first flow path 56a through which the intermediate medium M2 flows and the LN flow through the first flow path layer 56. The laminated body with the 2nd flow path layer 57 in which 2 flow paths (illustration omitted) were formed becomes the structure provided between the end plates 58 and 58. FIG. The upper end of the 1st flow path 56a is opened to the upper surface of a laminated body. The second channel extends in a direction orthogonal to the first channel 56a.

In the stacked heat exchanger E3a, headers 61 and 62 are provided on a pair of side surfaces facing opposite to each other. For example, the front header shown in FIG. 3 is the inflow side header 61 connected to the outlet pipe 32. On the side opposite to the inflow side header 61, an outflow side header 62 that collects and flows out NG flowing through the second flow path is provided. In the present embodiment, since it has a one-pass configuration, the headers 61 and 62 are divided into front and rear side surfaces. However, the configuration is not limited to one pass, and may be a configuration having two or more passes.

As in the case of the LNG evaporator E2, the stacked heat exchanger E3a is provided with a liquid reservoir 59 and a liquid seal tube 63. The liquid reservoir 59 is provided on the lower side of the laminate, and the liquid sealed tube 63 is connected to the bottom surface of the liquid reservoir 59. The liquid reservoir 59 is formed in a shape that covers the entire lower surface of the laminate so that its internal space communicates with all the first flow paths 56a. The liquid intermediate medium M2 stored in the liquid reservoir 59 closes the lower end of the first flow path 56a. The liquid seal tube 63 extends downward from the bottom surface of the liquid reservoir 59. The lower end portion of the liquid seal tube 63 is immersed in the intermediate medium M <b> 2 stored in the housing 52. Note that a gas layer may exist between the liquid intermediate medium M2 accumulated at the lower end portion in the first flow path 56a and the liquid intermediate medium M2 accumulated in the liquid reservoir 59, or The gas layer may not exist.

NG flows into the inflow side header 61 through the lead-out pipe 32 and is divided into the second flow paths through the inflow side header 61. The NG in each second flow path is heated by the intermediate medium M2 in the first flow path 56a. This NG flows into the outflow side header 62 and is then supplied to the user side through the discharge pipe 65.

Here, the operation of the vaporizer 10 according to the first embodiment will be described.

The liquid intermediate medium M stored in the lower part of the shell 11 is heated and evaporated by seawater flowing into the heat transfer tubes 20 through the intermediate chamber 14. Seawater flows out of the heat transfer pipe 20 and is discharged to the outside through the outlet chamber 18 and the discharge pipe 24.

The evaporated intermediate medium M exchanges heat with LNG in the LNG evaporator E2 located in the upper part of the shell 11. Specifically, in the LNG evaporator E2, heat exchange is performed between the intermediate medium M in the first flow path 41a and the LNG in the second flow path 42a, and the gaseous intermediate medium M is condensed. LNG evaporates. At this time, due to the condensation of the intermediate medium M, the pressure in the first flow path 41a is lower than the pressure around the microchannel heat exchanger. Since the lower side of the first flow path 41a is closed by the liquid intermediate medium M stored in the liquid reservoir 45 and the liquid seal tube 46, the first flow path 41a is stored in the liquid reservoir 45 and the liquid seal tube 46. The head (differential pressure) corresponding to the height difference between the liquid level of the liquid intermediate medium and the liquid level of the liquid intermediate medium accumulated in the intermediate medium evaporator E1 is intermediate to the first flow path 41a. It acts as an inflow suction force for the medium. For this reason, the gaseous intermediate medium M is sucked into the first flow path 41a through the opening at the upper end of the first flow path 41a and is not sucked from the lower end of the first flow path 41a. Thereby, a flow in a direction in which the intermediate medium M flows down occurs in the first flow path 41a. The intermediate medium M that has flowed down through the first flow path 41 a is stored in the liquid reservoir 45. In this manner, in the shell 11, the circulation of the intermediate medium M is repeated between the intermediate medium evaporator E1 and the LNG evaporator E2.

NG vaporized in the LNG evaporator E2 flows through the outlet pipe 32 via the outlet chamber 28 and is introduced into the heater E3. In the warmer E3, it flows into the 2nd flow path of the laminated heat exchanger E3a through the inflow side header 61 from the outlet tube 32. FIG. The NG in the second flow path is heated by the intermediate medium M <b> 2 flowing in the first flow path 56 a and supplied to the usage side via the outflow header 62 and the discharge pipe 65.

Also in the warmer E3, the intermediate medium M2 flows down from the top to the bottom in the first flow path 56a of the stacked heat exchanger E3a. That is, also in the laminated heat exchanger E3a of the heater E3, the liquid level of the liquid intermediate medium M2 stored in the liquid reservoir 59 and the liquid intermediate collected in the housing 52 are the same as in the LNG evaporator E2. A head (differential pressure) corresponding to the height difference from the liquid level of the medium M2 acts as an inflow and suction force of the intermediate medium M2 into the first flow path 56a.

As described above, in the present embodiment, since the LNG evaporator E2 includes the stacked heat exchanger, the LNG evaporator E2 is LNG as compared with the case where the LNG evaporator E2 is formed by a multi-tube heat exchanger. The evaporator E2 can be reduced in size and weight. Moreover, since the laminated heat exchanger is configured such that the intermediate medium M flows down by gravity in the first flow path 41a, the intermediate heat medium M is condensed in the first flow path 41a in the laminated heat exchanger. As a result, the pressure in the first flow path 41a decreases, so that the gaseous intermediate medium M easily flows into the first flow path 41a. Therefore, even in the case where the LNG evaporator E2 is configured by a stacked heat exchanger having the stacked body 38 in which the first flow path 41a and the second flow path 42a are formed, there is an intermediate in the first flow path 41a. There is no need to provide a means for pushing the medium M.

In addition, in the present embodiment, since the liquid reservoir 45 is provided in the LNG evaporator E2, the lower part of the first flow path 41a is blocked by the liquid intermediate medium M. For this reason, it is possible to prevent the intermediate medium M from flowing into the first flow path 41a from the downstream end. Therefore, since the intermediate medium M flows into the first flow path 41a from one direction, it becomes easy to obtain the flow of the intermediate medium M in the first flow path 41a. Therefore, the intermediate medium M can be easily circulated between the intermediate medium evaporator E1 and the LNG evaporator E2.

Furthermore, in this embodiment, a liquid seal tube 46 is provided to connect the liquid reservoir 45 and the liquid surface of the liquid intermediate medium M collected in the intermediate medium evaporator E1, and the liquid intermediate medium M is filled in the liquid seal tube 46. Has been. Therefore, the liquid intermediate medium M stored in the liquid reservoir 45 and the liquid intermediate medium M stored in the intermediate medium evaporator E1 are connected through the liquid seal tube 46. When the intermediate medium M condenses in the first flow path 41a and the pressure in the first flow path 41a decreases, the liquid level of the liquid intermediate medium M stored in the liquid reservoir 45; A head (differential pressure) according to the height difference from the liquid surface of the liquid intermediate medium M accumulated in the intermediate medium evaporator E1 acts as an inflow and suction force of the intermediate medium M into the first flow path 41a. . At this time, the distance between the liquid level in the liquid reservoir 45 and the liquid level in the intermediate medium evaporator E1 can be increased according to the length of the liquid seal tube 46. The suction force into the one flow path 41a can be further increased. Furthermore, since the liquid sealing tube 46 is connected to the liquid level in the intermediate medium evaporator E1, it is possible to suppress the evaporation surface of the intermediate medium M from being reduced as compared with the case where the liquid reservoir 45 is directly connected to the liquid level. be able to.

In this embodiment, the LNG evaporator E2 is disposed in the shell 11 of the intermediate medium evaporator E1. For this reason, the intermediate medium M circulates in the shell 11 between the intermediate medium evaporator E1 and the LNG evaporator E2. For this reason, the flow resistance until the intermediate medium M evaporated by the intermediate medium evaporator E1 is sucked into the first flow path 41a can be reduced. Therefore, natural circulation can be facilitated.

In the present embodiment, the stacked heat exchanger of the LNG evaporator E2 is a microchannel heat exchanger. For this reason, the LNG evaporator E2 can be reduced in size and weight.

In the above embodiment, the configuration in which the liquid reservoir 45 and the liquid seal tube 46 are provided has been described. However, as shown in FIG. 4, the liquid reservoir 45 and the liquid seal tube 46 are omitted, and the LNG evaporator E2 is an intermediate medium. You may arrange | position above the liquid level of M. Alternatively, as illustrated in FIG. 5, only the liquid sealing tube 46 may be omitted, and the LNG evaporator E2 and the liquid reservoir 45 may be disposed above the liquid level of the intermediate medium M.

Further, as shown in FIG. 6, the liquid seal tube 46 may be omitted, and the liquid reservoir 45 may be in direct contact with the intermediate medium M stored in the intermediate medium evaporator E1. In this configuration, the intermediate medium M in the liquid reservoir 45 and the intermediate medium M accumulated in the intermediate medium evaporator E1 are connected through an opening formed in the liquid reservoir 45. Therefore, even in this embodiment, the difference in height between the liquid level of the liquid intermediate medium M stored in the liquid reservoir 45 and the liquid level of the liquid intermediate medium M stored in the intermediate medium evaporator E1 does not increase. The suction force of the intermediate medium M according to the head (differential pressure) according to the difference can be obtained.

Further, the liquid seal tube 63 provided in the stacked heat exchanger E3a in the heater E3 can be omitted in the same manner, and the liquid reservoir 59 in the heater E3 is also directly in the heater E3. Can be immersed in the liquid surface of the intermediate medium M2. Further, the liquid reservoir 59 may be omitted.

In the above-described embodiment, the heater E3 is configured as an intermediate medium heat exchanger and the stacked heat exchanger E3a is provided. However, the present invention is not limited thereto. For example, as shown in FIG. 7, the laminated heat exchanger E3a is omitted, and NG introduced into the casing 52 of the heater E3 through the outlet pipe 32 and, for example, seawater that is a heat source medium flowing in the heat transfer pipe May be configured to directly exchange heat. In this configuration, the heater E3 is configured as a multi-tube heat exchanger in which the inside of the casing 52 is filled with NG and the heat transfer tubes are disposed therein.

In the above embodiment, the heater E3 is provided, but the heater E3 may be omitted. In this case, the intermediate chamber 14 is also unnecessary.

(Second Embodiment)
FIG. 8 shows a second embodiment of the present invention. In addition, although it demonstrates concretely below, the same code | symbol is attached | subjected to the same component as 1st Embodiment here, and the detailed description is abbreviate | omitted.

In the first embodiment, the LNG evaporator E2 is arranged in the shell 11 of the intermediate medium evaporator E1, whereas in the second embodiment, the LNG evaporator E2 is a shell 67 of the intermediate medium evaporator E1. And a circulation pipe 66 that connects the LNG evaporator E2 and the intermediate medium evaporator E1 to each other. The circulation pipe 66 extends into the shell 67 from the first pipe 66a that connects the upper surface of the shell 67 of the intermediate medium evaporator E1 and the upper surface of the header 68 (described later) of the LNG evaporator E2, and the lower surface of the liquid reservoir 45. And a second pipe 66b.

The intermediate medium evaporator E1 includes a large number of heat transfer tubes 20 provided in the shell 67. The shell 67 is filled with the liquid intermediate medium M to a position where all the heat transfer tubes 20 are immersed.

The LNG evaporator E2 has a configuration in which a liquid reservoir 45 is provided on the lower surface and a header 68 is provided on the upper surface. The lower surface of the header 68 is formed in an open hollow shape. On the upper surface of the header 68, an inlet for introducing the intermediate medium M flowing through the first pipe 66a is formed. The gaseous intermediate medium M that has flowed into the header 68 through the introduction port flows into the first flow paths 41 a in the stacked body 38. In the present embodiment, the LNG evaporator E2 is configured by a microchannel heat exchanger, but is not limited thereto, and may be configured by, for example, a plate fin heat exchanger.

The second pipe 66b functions as a liquid seal pipe. The second pipe 66b extends to the inside of the shell 67, and the lower end of the second pipe 66b is located below the liquid level of the liquid intermediate medium M in the intermediate medium evaporator E1. That is, the liquid intermediate medium M is filled from the liquid level in the intermediate medium evaporator E1 to the second pipe 66b and the liquid reservoir 45.

In the present embodiment, also in the heater E3, the laminated heat exchanger E3a is provided outside the housing 70 of the heat transfer tube heat exchanger E3b. That is, the warmer E3 is configured by an intermediate medium type heat exchanger, and a heat transfer tube heat exchanger E3b that exchanges heat between the heat source medium (for example, seawater) and the intermediate medium M2, and the intermediate medium M2 and NG. And a connection pipe 69 that connects the heat transfer tube heat exchanger E3b and the multilayer heat exchanger E3a to each other. The connection pipe 69 includes a first connection pipe 69a that connects the upper surface of the housing 70 of the heat transfer tube heat exchanger E3b and the upper surface of a header 72 (described later) of the stacked heat exchanger E3a, and a lower surface of the liquid reservoir 59. It has the 2nd connection piping 69b extended to the liquid level in the housing | casing 70 of the heat exchanger tube type heat exchanger E3b.

The heat transfer tube heat exchanger E <b> 3 b has a large number of heat transfer tubes 54 disposed in the housing 70, and for example, seawater as a heat source medium flows in the heat transfer tubes 54. The casing 70 is filled with the liquid intermediate medium M2 up to a position where all the heat transfer tubes 54 are immersed.

The laminated heat exchanger E3a has a configuration in which a liquid reservoir 59 is provided on the lower surface and a header 72 is provided on the upper surface. The lower surface of the header 72 is formed in an open hollow shape. On the upper surface of the header 72, an introduction port for introducing the intermediate medium M flowing through the first connection pipe 69a is formed. The gaseous intermediate medium M that has flowed into the header 72 through the introduction port flows into the first flow paths 56a in the laminated body.

In the present embodiment, the stacked heat exchanger E3a is configured by a microchannel heat exchanger, but is not limited thereto, and may be configured by, for example, a plate fin heat exchanger.

In the second embodiment, in the LNG evaporator E2, when the liquid intermediate medium M exchanges heat with LNG, it condenses. As a result, the pressure in the first flow path 41a of the LNG evaporator E2 is reduced, so that the gaseous intermediate medium M evaporated in the intermediate medium evaporator E1 is sucked into the LNG evaporator E2 through the first pipe 66a. . The liquid intermediate medium M condensed in the LNG evaporator E 2 is stored in the liquid reservoir 45. Since the liquid intermediate medium M is also stored in the second pipe 66b, the lower side of the first flow path 41a is blocked with the liquid intermediate medium M. Therefore, the force that the liquid intermediate medium M in the liquid reservoir 45 and the second pipe 66b tries to lower acts as a suction force for the gaseous intermediate medium M into the first flow path 41a. As a result, the intermediate medium M flows from the first pipe 66a into the LNG evaporator E2.

NG gasified in the LNG evaporator E2 is introduced into the stacked heat exchanger E3a of the heater E3 through the outlet pipe 32. NG is heated by the intermediate medium M2 in the stacked heat exchanger E3a and supplied to the use side. In the same manner as the circulation of the intermediate medium M between the intermediate medium evaporator E1 and the LNG evaporator E2, the natural circulation of the intermediate medium M2 also occurs between the stacked heat exchanger E3a and the heat transfer tube heat exchanger E3b.

According to the second embodiment, the shell 67 of the intermediate medium evaporator E1 can be reduced in size. Further, when the laminated heat exchanger (LNG evaporator E2) is abnormal, the intermediate medium evaporator E1 does not get in the way, so that it is easy to check and the like.

In the second embodiment, the second pipe 66b extends to the inside of the shell 67, and the lower end of the second pipe 66b is positioned below the liquid level of the liquid intermediate medium M in the intermediate medium evaporator E1. However, the lower end of the second pipe 66b may be positioned above the liquid level of the intermediate medium M. In this case, the second pipe 66b does not function as a liquid seal pipe. The same applies to the heat transfer tube heat exchanger E3b of the heater E3. That is, the second connection pipe 69b extends to the inside of the casing 70, and the lower end of the second connection pipe 69b is below the liquid level of the liquid intermediate medium M2 in the casing 70 of the heat transfer tube heat exchanger E3b. However, the lower end of the second connection pipe 69b may be positioned above the liquid level of the liquid intermediate medium M2.

In the second embodiment, the heater E3 may be configured as a multi-tubular heat exchanger E3b, similarly to the configuration of FIG. That is, as shown in FIG. 9, the laminated heat exchanger E3a that constitutes the warmer E3 may be omitted, and seawater and NG that are heat source media may directly exchange heat in the heat transfer tubes.

Although the description of other configurations, operations, and effects is omitted, they are the same as those in the first embodiment and its modifications.

Here, the intermediate medium vaporizer of the above embodiment will be outlined.

The intermediate medium vaporizer includes an intermediate medium evaporation unit that evaporates at least a part of the intermediate medium by heat exchange between a heat source medium and a liquid intermediate medium, and an intermediate medium evaporated by the intermediate medium evaporation unit. And a liquefied gas vaporization section that vaporizes the low-temperature liquefied gas by condensing to flow out the gas, and the liquefied gas vaporization section has a first flow path layer having a first flow path that is a flow path of the intermediate medium. And a laminated heat exchanger having a laminated body in which a second flow path layer having a second flow path that is a flow path of a low-temperature liquefied gas is laminated, and the laminated heat exchanger includes the first flow The first flow path is installed in a posture extending in a vertical direction or a direction inclined with respect to the vertical direction so that the intermediate medium flows down by gravity in the path.

In this intermediate medium type vaporizer, the liquefied gas vaporization section is constituted by a laminated heat exchanger, so that the liquefied gas vaporization section is compared with the case where the liquefied gas vaporization section is formed by a multi-tubular heat exchanger. The part can be reduced in size and weight. Moreover, since the laminated heat exchanger is configured such that the intermediate medium flows down by gravity in the first flow path, the laminated heat exchanger is accompanied by the condensation of the intermediate medium in the first flow path. As the pressure in the first flow path decreases, the gaseous intermediate medium easily flows into the first flow path. Therefore, even when the liquefied gas vaporization unit is configured by a stacked heat exchanger having a stacked body in which the first flow path and the second flow path are formed, the intermediate medium is pushed into the first flow path. There is no need to provide means. From this point, the intermediate medium type vaporizer can be reduced in weight.

The liquefied gas vaporization unit may be provided with a liquid reservoir in which a liquid intermediate medium is stored downstream of the first flow path.

In this aspect, it is possible to prevent the gaseous intermediate medium from flowing into the first flow path from the downstream end of the first flow path. Therefore, since the intermediate medium flows into the first flow path from one direction, formation of a flow toward the lower side of the intermediate medium in the first flow path is promoted. Therefore, the intermediate medium can be easily circulated between the intermediate medium evaporation section and the liquefied gas vaporization section.

The intermediate medium evaporation unit may be located below the liquefied gas vaporization unit. In this case, the intermediate medium type vaporizer may further include a liquid seal tube that connects the liquid reservoir and a liquid surface of the liquid intermediate medium accumulated in the intermediate medium evaporation section.

In this aspect, the liquid sealed medium is filled with the liquid intermediate medium, and the liquid intermediate medium stored in the liquid reservoir and the liquid intermediate medium stored in the intermediate medium evaporation unit are connected through the liquid sealed pipe. . When the pressure in the first flow path decreases as the intermediate medium condenses in the first flow path, the liquid surface of the liquid intermediate medium stored in the liquid reservoir and the intermediate medium evaporation section A head (differential pressure) corresponding to the height difference from the liquid level of the accumulated liquid intermediate medium acts as an inflow and suction force of the intermediate medium into the first flow path. At this time, since the distance between the liquid level in the liquid reservoir and the liquid level in the intermediate medium evaporation unit can be increased according to the length of the liquid seal tube, the first flow path is set according to this distance. The suction force to the inside can be further increased. Further, since the liquid level in the liquid reservoir and the liquid level of the intermediate medium evaporation unit are connected by the liquid seal tube, the intermediate medium evaporation unit has an intermediate position compared to the case where the liquid reservoir directly contacts the liquid level of the intermediate medium evaporation unit. It can suppress that the evaporation surface of a medium decreases.

The liquefied gas vaporization unit may be disposed in a shell of the intermediate medium evaporation unit.

In this aspect, the intermediate medium circulates between the intermediate medium evaporation section and the liquefied gas vaporization section in the shell. For this reason, the flow resistance until the intermediate medium evaporated in the intermediate medium evaporation section is sucked into the first flow path can be reduced. Therefore, natural circulation can be facilitated.

The liquefied gas vaporization section is provided outside the shell of the intermediate medium evaporation section, and the intermediate medium vaporizer further includes a circulation pipe that connects the liquefied gas vaporization section and the shell of the intermediate medium evaporation section. May be. In this aspect, the shell of the intermediate medium evaporation unit can be reduced in size. In addition, when the laminated heat exchanger is abnormal, the intermediate medium evaporation section does not get in the way, so that the laminated heat exchanger can be easily inspected.

The stacked heat exchanger may be a microchannel heat exchanger. In this aspect, the liquefied gas vaporization part can be reduced in size and weight. Here, the microchannel heat exchanger is a heat exchanger provided with a laminate formed by laminating a large number of metal plates having excellent heat transfer characteristics. In this laminated body, a flow path layer made of a metal plate in which a flow path through which an intermediate medium flows is recessed and a flow path layer made of a metal plate in which a flow path through which a low-temperature liquefied gas flows are alternately stacked. It becomes the composition. The channels formed in these metal plates have a channel width of 0.2 mm to 3 mm, for example.

Claims (6)

An intermediate medium evaporation section that evaporates at least a part of the intermediate medium by heat exchange between the heat source medium and the liquid intermediate medium;
A liquefied gas vaporizing unit that condenses the intermediate medium evaporated in the intermediate medium evaporating unit to evaporate the low-temperature liquefied gas and flow out the gas;
The liquefied gas vaporization unit is formed by laminating a first flow path layer having a first flow path that is a flow path for an intermediate medium and a second flow path layer having a second flow path that is a flow path for a low-temperature liquefied gas. It is constituted by a laminated heat exchanger having a laminated body,
The stacked heat exchanger is installed in a posture in which the first flow path extends in a vertical direction or a direction inclined with respect to the vertical direction so that the intermediate medium flows down by gravity in the first flow path. Intermediate medium vaporizer. 2. The intermediate medium vaporizer according to claim 1, wherein the liquefied gas vaporizer is provided with a liquid reservoir in which a liquid intermediate medium is accumulated downstream of the first flow path. A liquid seal tube that connects the liquid reservoir and the liquid surface of the liquid intermediate medium accumulated in the intermediate medium evaporation section;
The intermediate medium vaporizer according to claim 2, wherein the intermediate medium evaporation unit is located below the liquefied gas vaporization unit. The intermediate medium evaporation unit has a shell for accommodating the intermediate medium,
4. The intermediate medium type vaporizer according to claim 1, wherein the liquefied gas vaporization unit is disposed in a shell of the intermediate medium evaporation unit. 5. A circulation pipe for connecting the intermediate medium evaporation section and the liquefied gas vaporization section;
The intermediate medium evaporation unit has a shell for accommodating the intermediate medium,
The liquefied gas vaporization unit is provided outside the shell of the intermediate medium evaporation unit,
The intermediate medium vaporizer according to claim 1, wherein the circulation pipe connects a shell of the intermediate medium evaporation unit and the liquefied gas vaporization unit. The intermediate medium type vaporizer according to claim 1, wherein the stacked heat exchanger is a microchannel heat exchanger.

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