JP2016180552A - Heat exchanger and liquefied gas evaporator - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a layered type heat exchanger that is compact and can restrain a temperature difference between adjacent flow passage layers from becoming too large.SOLUTION: A liquefied gas evaporator 100 comprises a core 1 having a layered structure in which a plurality of planar flow passage layers 2 are layered, and including a first flow passage part 10 through which first fluid 7 is passed, and a second flow passage part 20 through which second fluid 8 is passed. The flow passage layers 2 of the first flow passage 10 include an introduction flow passage layer 11 comprising an inlet 11a, and discharge flow passage layers 12 comprising outlets 12a, and the first flow passage part 10 has a folded flow passage shape. The flow passage layers 2 of the second flow passage part 20 include adjacent flow passage layers 21 adjacent to the discharge flow passage layers 12 of the first flow passage 10 on the outside of the first flow passage 10.SELECTED DRAWING: Figure 3

Description

  The present invention relates to a heat exchanger and a liquefied gas evaporator, and more particularly to a heat exchanger and a liquefied gas evaporator that perform heat exchange between a first fluid and a second fluid.

  Conventionally, a liquefied gas evaporator that performs heat exchange between a first fluid and a second fluid is known (see, for example, Patent Document 1).

  Patent Document 1 discloses an open rack type liquefied gas evaporator provided with a heat transfer tube having a double tube structure. In this liquefied gas evaporator, a liquefied gas is used as the first fluid, and a heat medium such as seawater is used as the second fluid. The heat transfer tube introduces a cryogenic liquefied gas into the inner tube of the double tube, folds the liquefied gas from the open end on one end side of the inner tube to the outer tube (the passage between the inner tube and the outer tube), It is comprised so that it may lead out from the other end side of an outer tube. The heat medium (seawater) is poured from the watering trough to the outside of the heat transfer tube (outer tube). The liquefied gas evaporates by exchanging heat with the heat medium when flowing through the outer tube, and is led out from the heat transfer tube (outer tube) in a gas phase. Further, the heat exchange between the liquefied gas passing through the inner pipe and the liquefied gas passing through the outer pipe reduces the temperature difference between the liquefied gas and the heat medium when the liquefied gas reaches the outer pipe, and the outer pipe Freezing of the heat medium (seawater) on the surface is suppressed.

JP-A-5-332499

  However, since the liquefied gas evaporator of Patent Document 1 has an open rack type structure in which a heat medium (second fluid) is passed through the heat transfer tubes, there is a problem that the apparatus becomes large. In addition, since the heat medium (second fluid) is supplied in an open state, it is difficult to mount the liquefied gas evaporator on a moving body such as a ship, a vehicle, or an airplane. There is a point.

  On the other hand, a heat exchanger having a laminated structure having a layered flow path such as a plate fin type can realize a small and non-open flow path configuration. However, when the temperature difference between the first fluid (liquefied gas) and the second fluid (seawater) is large as in Patent Document 1, the temperature difference between adjacent flow paths becomes large in the laminated heat exchanger. The problem of too much occurs.

  That is, when a heat exchanger having a laminated structure is used for a liquefied gas evaporator, the flow of the second fluid side is caused by freezing of the second fluid as a result of heat exchange between the cryogenic first fluid and the second fluid as the heat medium. The road may be blocked. For example, when the second fluid is evaporated or heated by the high-temperature first fluid, a large thermal stress is generated between adjacent flow path layers due to the temperature difference, and it is difficult to reduce the size. Therefore, it is difficult to use a heat exchanger having a laminated structure for heat exchange between fluids having a large temperature difference.

  The present invention has been made in order to solve the above-described problems, and one object of the present invention is small and can suppress the temperature difference between adjacent flow path layers from becoming too large. It is to provide a stacked heat exchanger and a liquefied gas evaporator.

  To achieve the above object, a heat exchanger according to a first aspect of the present invention has a laminated structure in which a plurality of planar flow passage layers are laminated, and includes a first flow passage section for circulating a first fluid, A heat exchange section including a second flow path section through which fluid flows, and the flow path layer of the first flow path section includes an introduction flow path layer having an inlet and an outer outlet flow path layer having an outlet. The first channel portion has a folded channel shape, and the channel layer of the second channel portion is adjacent to the outlet channel layer of the first channel portion outside the first channel portion. Includes adjacent channel layer. The “folded flow path shape” is not limited to the flow path shape folded once so as to include two layers of the introduction flow path layer and the discharge flow path layer, but also the introduction flow path layer and the discharge flow path layer. A flow path shape that is bent back and forth so as to include one or a plurality of intermediate flow path layers.

  In the heat exchanger according to the first aspect of the present invention, as described above, the first flow path section that causes the first fluid to flow through the heat exchange section having a laminated structure in which a plurality of planar flow path layers are stacked, A heat exchanger can be reduced in size by providing the 2nd flow-path part which distribute | circulates 2 fluids. In addition, since the first flow path portion and the second flow path portion can be configured by a planar closed flow path layer, unlike an open rack structure in which fluid is supplied to the outside, the mobile body Can be easily mounted. Further, by configuring the first flow path portion to have a folded flow path shape, the first fluid is adjacent to the first flow path while passing through the folded flow path from the introduction flow path layer to the discharge flow path layer. The temperature of the first fluid is gradually brought closer to the temperature of the second fluid by heat exchange between the first fluids flowing through the flow path layer, and the first fluid flows in the outer lead-out flow path layer after approaching the temperature of the second fluid. And heat exchange with the second fluid flowing in the adjacent flow path portion. As a result, even if a heat exchange part having a laminated structure is employed, the temperature difference between the first fluid and the second fluid between the adjacent outlet channel layer and the adjacent channel layer can be reduced. As a result of the above, according to the present invention, it is possible to provide a stacked heat exchanger that is small in size and can suppress a temperature difference between adjacent flow path layers from becoming too large.

  In the heat exchanger according to the first aspect of the present invention, preferably, the first fluid is a low-temperature side fluid, the second fluid is a high-temperature side fluid, and the heat exchange portion is a first fluid flowing through the second flow path portion. The first fluid flowing through the first flow path is heated by heat exchange with the two fluids. If comprised in this way, it heats up gradually while the 1st fluid of the low temperature side is folded in the 1st flow path part, and it is made to heat-exchange between the 1st fluid after the temperature rises, and the 2nd fluid Can do. As a result, even when the supply temperature of the first fluid is extremely low, it can be suppressed that the second fluid on the high temperature side freezes and the adjacent flow path layer is blocked.

  In the heat exchanger according to the first aspect of the present invention, preferably, the first flow path section evaporates the first fluid that has flowed into the introduction flow path layer in a state including the liquid phase, and the gas of the first fluid in the gas phase state From the outlet channel layer. If comprised in this way, the liquefied gas evaporator which evaporates the 1st fluid which flows in into an introductory channel layer in a liquid phase state, and makes it flow out from an outlet channel layer in a gas state can be constituted. Even in this case, since the temperature difference between the first fluid (liquefied gas) and the second fluid (heat medium) can be suppressed by the first flow path portion having the folded structure, the heat exchanger as the liquefied gas evaporator can be easily reduced in size. Can be

  In the heat exchanger according to the first aspect of the present invention, preferably, the gas phase gas obtained by evaporating the first fluid from the introduction flow path layer to the discharge flow path layer flows into the discharge flow path layer. The number of turns of one flow path portion is set. If comprised in this way, since the temperature of the 1st fluid (liquefied gas) at the time of flowing in into the derivation | leading-out flow path layer can be reliably raised more than evaporation temperature, it is effective in the 2nd in an adjacent flow path layer. Blockage of the flow path due to icing of the fluid can be suppressed.

  In the heat exchanger according to the first aspect of the present invention, preferably, the introduction flow path layer is disposed at the center in the stacking direction in the first flow path section, and the lead-out flow path layer is both in the stacking direction in the first flow path section. Each of the first flow passage portions has a branched flow passage shape branched from the central introduction flow passage layer and folded, and the second flow passage portion has the first flow passage in the stacking direction. It is comprised by the adjacent flow path layer adjacent to each derivation | leading-out flow path layer in the both outer sides of a part. If comprised in this way, since heat exchange with a 1st fluid and a 2nd fluid can be performed on both sides of a lamination direction, respectively, the heat-transfer area of a 1st fluid and a 2nd fluid can be enlarged. Moreover, since the introduction flow path layer through which the first fluid in the highest temperature or the lowest temperature flows can be arranged in the center of the heat exchange part, it is possible to suppress the outer surface temperature of the heat exchange part from becoming too high or low.

  In the heat exchanger according to the first aspect of the present invention, preferably, the first flow path part further includes a partition member that partitions each of the stacked flow path layers and has a through hole penetrating in the stacking direction. The passage portion has a flow path shape that is folded over a plurality of flow path layers through the through holes of the partition member. If comprised in this way, the flow-path shape turned up inside the 1st flow-path part (heat exchange part) is realizable. As a result, for example, the heat exchanger can be made smaller compared to a structure in which the first fluid is drawn out from one channel layer and introduced into the other channel layer. In addition, when the first fluid is drawn out, the outer surface of the drawn flow path portion may be too hot or cold, and in the present invention, the outer surface temperature of the heat exchange unit is high or low. It is possible to suppress the temperature from becoming too low.

  In the heat exchanger according to the first aspect of the present invention, preferably, the first flow path part and the second flow path part are made of a material having a thermal conductivity of 50 W / (m × K) or less. If comprised in this way, the heat conductivity of a 1st flow path part and a 2nd flow path part will become low compared with the material of high heat conductivity like aluminum (about 195 W / m * K), for example. Therefore, it is possible to suppress the flow path surface temperature on the adjacent flow path layer side adjacent to the outlet flow path layer through which the first fluid flows from being excessively deviated from the temperature of the second fluid. As a result, it is possible to suppress the temperature difference between the adjacent outlet channel layer and the adjacent channel layer from becoming too large easily and effectively.

  The liquefied gas evaporator according to the second invention has a laminated structure in which a plurality of planar flow path layers are laminated, and a liquefied gas flow path section through which a liquefied gas flows and a heat medium flow path section through which a heat medium flows. The liquefied gas channel section includes a lead channel layer having an inlet and an outer outlet channel layer having an outlet, and the liquefied gas channel section is folded back. The flow path layer of the heat medium flow path section includes an adjacent flow path layer adjacent to the outlet flow path layer of the liquefied gas flow path section outside the liquefied gas flow path section.

  In the liquefied gas evaporator according to the second invention, as described above, the liquefied gas flow path section and the heat medium flow path section are provided in the stacked heat exchange section in which a plurality of planar flow path layers are stacked. As a result, the liquefied gas evaporator can be reduced in size. In addition, since the liquefied gas flow path section and the heat medium flow path section can be configured by a planar closed flow path layer, unlike the open rack structure, it can be easily mounted on a moving body. Furthermore, by configuring the liquefied gas flow path portion so as to have a folded flow path shape, the liquefied gas is adjacent while passing through the folded flow path from the introduction flow path layer to the discharge flow path layer. The temperature of the liquefied gas is gradually increased by heat exchange between the liquefied gases flowing in the flow path layer, and the heat exchange between the liquefied gas and the heat medium flowing in the heat medium flow path section is performed in the outer discharge flow path layer after the temperature rises. It can be performed. As a result, even if a heat exchange section having a laminated structure is employed, the temperature difference between the liquefied gas and the heat medium between the adjacent outlet channel layer and the adjacent channel layer can be reduced. For this reason, the blockage | closure of the flow path by the freezing of the 2nd fluid in an adjacent flow path layer can be suppressed. As a result, according to the present invention, it is possible to provide a stacked liquefied gas evaporator that is small in size and can suppress the temperature difference between adjacent flow path layers from becoming too large.

  According to the present invention, as described above, it is possible to provide a stacked heat exchanger and a liquefied gas evaporator that are small and can suppress a temperature difference between adjacent flow path layers from becoming too large. .

It is the perspective view which showed the liquefied gas evaporator by 1st Embodiment of this invention. It is a longitudinal cross-sectional view of the direction orthogonal to the flow path of the liquefied gas evaporator by 1st Embodiment of this invention. It is a longitudinal cross-sectional view of the direction along the flow path of the liquefied gas evaporator by 1st Embodiment of this invention. It is the figure which showed the simulation result of the temperature distribution of the liquefied gas evaporator by 1st Embodiment of this invention. It is the schematic diagram which showed the heat exchanger by 2nd Embodiment of this invention. It is the schematic diagram which showed the 2nd modification of the heat exchanger by 3rd Embodiment of this invention. It is the schematic diagram which showed the 1st modification of the liquefied gas evaporator by 1st Embodiment of this invention. It is the schematic diagram which showed the 2nd modification of the liquefied gas evaporator by 1st Embodiment of this invention.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings.

[First Embodiment]
First, the configuration of the liquefied gas evaporator 100 according to the first embodiment will be described with reference to FIGS. The liquefied gas evaporator 100 is an example of the “heat exchanger” in the present invention.

(Overall configuration of liquefied gas evaporator)
A liquefied gas evaporator 100 shown in FIG. 1 is an apparatus (heat exchanger) for evaporating a low-temperature liquefied gas by heat exchange with a heat medium and supplying it as a gas in a gas phase state. The liquefied gas evaporator 100 is mounted on a moving body such as a ship, a vehicle, and an airplane.

  The liquefied gas is, for example, oxygen, nitrogen or natural gas. The heat medium used in the liquefied gas evaporator varies, but from the viewpoint of easy availability (low cost), water, seawater, air, etc., which are abundant even in installation environments such as moving bodies, are used. It is done. While these water or seawater and air are easily available, they are heat media having the property of freezing at a temperature higher than the supply temperature of the liquefied gas. Moreover, water or seawater and air are heat media having a property of corroding a metal material constituting the flow path of the liquefied gas evaporator. The liquefied gas evaporator 100 of the first embodiment is configured to use water, seawater, air, or the like having such properties as a heat medium.

  In the first embodiment, the liquefied gas evaporator 100 includes a plate fin type core 1. The plate fin-type core 1 is a heat exchange part having a laminated structure in which a plurality of planar flow path layers 2 are laminated. The core 1 is an example of the “heat exchange part” in the present invention.

  As shown in FIG. 2, the flow path layer 2 constituting the core 1 has a planar shape including corrugated fins 3 constituting individual flow paths (channels) and side bars 4 constituting the outer peripheral wall of the corrugated fins 3. It has a (flat plate) structure. Each flow path layer 2 is partitioned by a tube plate 5 that is a partition wall in the stacking direction. The tube plate 5 and the corrugated fins 3 function as heat transfer surfaces that transfer heat within the core 1. The core 1 is formed in a rectangular box shape (cuboid shape) as a whole by sandwiching the laminated body of the flow path layers 2 between a pair of side plates 6 and joining them by brazing or the like.

  The core 1 includes a first flow path portion 10 that circulates the first fluid 7 and a second flow path portion 20 that circulates the fluid of the second fluid 8. In the first embodiment, the first fluid 7 is a low temperature side fluid, and the second fluid 8 is a high temperature side fluid. That is, the first fluid 7 is a liquefied gas, and the second fluid 8 is a heat medium. The first flow path part 10 and the second flow path part 20 are each composed of a plurality of flow path layers 2. The first fluid 7 is an example of the “cold side fluid” and “liquefied gas” in the present invention. The second fluid 8 is an example of the “high temperature side fluid” and the “heating medium” in the present invention. The first flow path part 10 and the second flow path part 20 are examples of the “liquefied gas flow path part” and the “heat medium flow path part” of the present invention, respectively.

  The core 1 exchanges heat between the first fluid 7 on the low temperature side flowing through the first flow path portion 10 and the second fluid 8 on the high temperature side flowing through the second flow path portion 20. In the first embodiment, the core 1 is configured to raise the temperature of the first fluid 7 that flows through the first flow path portion 10 by heat exchange with the second fluid 8 that flows through the second flow path portion 20. ing. As a result of the heat exchange, the first fluid 7 is evaporated by the heat contained in the second fluid 8 and supplied to the outside as a gas 7a in a gas phase state.

  In the first embodiment, the first flow path part 10 and the second flow path part 20 of the core 1 are made of a material having a thermal conductivity of 50 W / (m × K) or less. For example, the first flow path part 10 and the second flow path part 20 are made of a stainless steel material having a thermal conductivity of 50 W / (m × K) or less and having corrosion resistance. Specifically, SUS304, SUS304L SUS316, SUS316L, etc. can be used.

(Structure of the first flow path part)
As shown in FIG. 3, in the first embodiment, the first flow path unit 10 includes five flow path layers 2. The flow path layer 2 of the first flow path section 10 includes an introduction flow path layer 11 having an inlet 11a, an outer outlet flow path layer 12 having an outlet 12a, and an intermediate flow path layer 13. The first flow path unit 10 evaporates the first fluid 7 that has flowed into the introduction flow path layer 11 in a state including the liquid phase, and causes the gas 7 a of the first fluid 7 in the gas phase state to flow out from the outlet flow path layer 12. It is configured as follows. Each flow path layer 2 of the first flow path section 10 has a flow path width W (see FIG. 2), a flow path height (thickness) H1 (see FIG. 2), and a flow path length L, and has substantially the same shape. It is configured. In the first embodiment, as will be described later, the first flow path portion 10 has a flow path shape that is folded by each flow path layer 2.

  The introduction flow path layer 11 is disposed in the center of the first flow path portion 10 in the stacking direction Z. That is, the introduction flow path layer 11 is a flow path layer arranged in the third layer in the center among the five flow path layers 2. In the introduction flow path layer 11, the flow path is opened to the outside at the inlet 11 a at one end on the X1 direction side, and the outer peripheral portion except the inlet 11 a is closed by the side bar 4. A header tank (not shown) or the like is attached to the inlet 11a, and the first fluid 7 is supplied from the outside through the header tank.

  The lead-out flow path layers 12 are respectively disposed on both outermost sides in the stacking direction Z in the first flow path portion 10. That is, the lead-out flow path layer 12 is two flow path layers respectively disposed on the outermost first layer and the fifth layer among the five flow path layers 2. The two lead-out flow path layers 12 each have a flow path opened to the outside at the outlet 12a at the other end on the X2 direction side, and the outer peripheral portion excluding the outlet 12a is closed by the side bar 4. A header tank or the like (not shown) is attached to the outlet 12a, and the gas 7a that has been vaporized by the evaporation of the first fluid 7 is discharged through the header tank.

  The intermediate flow path layer 13 is disposed between the introduction flow path layer 11 and the discharge flow path layer 12 in the first flow path portion 10. That is, the intermediate flow path layer 13 is two flow path layers respectively disposed in the second and fourth layers of the five flow path layers 2. Each of the two intermediate flow path layers 13 is closed by the side bar 4 at the outer periphery over the entire circumference. Each intermediate flow path layer 13 is opened only to the flow path layer 2 adjacent in the stacking direction Z by a through hole 15 of a partition member 14 described later.

  In the first embodiment, the first flow path unit 10 includes a partition member 14 that partitions each of the stacked flow path layers 2 and has a through hole 15 penetrating in the stacking direction Z. The partition member 14 is a tube plate 5 provided with a through-hole 15 and is substantially the same as the tube plate 5, but the tube plate provided with the through-hole 15 is separated from the partition member 14 for distinction. A tube plate 5 having no through hole 15 is used. The partition member 14 is provided between the introduction flow path layer 11 and the intermediate flow path layer 13 and between the intermediate flow path layer 13 and the outlet flow path layer 12.

  In the partition member 14 a between the introduction flow path layer 11 and the intermediate flow path layer 13, a through hole 15 is disposed on the other end side in the X2 direction. Thereby, the introduction flow path layer 11 and the intermediate flow path layer 13 communicate with each other at the end in the X2 direction (the other end side). In the partition member 14b between the intermediate flow path layer 13 and the outlet flow path layer 12, a through hole 15 is disposed on one end side in the X1 direction. Thereby, the intermediate | middle flow path layer 13 and the derivation | leading-out flow path layer 12 are connected in the edge part of a X1 direction (one end side).

  As a result, in the first flow path section 10, one flow path layer 2 and the other flow path layer 2 are connected to each other through the through hole 15 at one end (X1 side end) or the other end (X2 side end). Communicate with each other. Thereby, the first flow path portion 10 has a flow path shape that is folded over the plurality of flow path layers 2 through the through holes 15 of the partition member 14. Further, the introduction flow path layer 11 communicates with the upper and lower intermediate flow path layers 13 through the through holes 15 at the other end (X2 side end portion). That is, the first flow path unit 10 has a branched flow path shape that is branched from the central introduction flow path layer 11 up and down.

  Here, in the first embodiment, the gas phase gas 7a in which the first fluid 7 evaporates between the introduction flow path layer 11 and the discharge flow path layer 12 flows into the discharge flow path layer 12. The number of turns of one flow path unit 10 is set. In other words, the first fluid 7 evaporates into a gas phase state from the introduction channel layer 11 to the outlet channel layer 12 through the intermediate channel layer 13 and flows as a gas phase gas 7a. It flows into the road layer 12. The number of intermediate flow path layers 13 (= the number of turns) is set so that the first fluid 7 is turned back as many times as necessary to flow into the outlet flow path layer 12 as the gas 7a in the gas phase. In the example shown in FIG. 3, the number of turns of the first flow path portion 10 between the introduction flow path layer 11 and the discharge flow path layer 12 is set to 2 times (up and down twice). In other words, the number of times of folding is a total of two times, the folding from the introduction channel layer 11 to the intermediate channel layer 13 and the folding from the intermediate channel layer 13 to the outlet channel layer 12. The required number of turns depends on the type and temperature of the first fluid 7 and the second fluid 8, the structure of the core 1, the use conditions, and the like, and therefore is determined by calculation (simulation) based on specific conditions (specifications). Is done.

(Structure of the second flow path part)
As shown in FIG. 3, the second flow path portion 20 includes two flow path layers 2. The channel layer 2 of the second channel unit 20 includes an adjacent channel layer 21 that is adjacent to the outlet channel layer 12 of the first channel unit 10 outside the first channel unit 10.

  In the first embodiment, since the outlet channel layer 12 of the first channel unit 10 is provided on both outer sides (first layer and fifth layer) of the first channel unit 10, the adjacent channel layer 21 is provided. Are provided corresponding to each lead-out flow path layer 12. That is, the second flow path portion 20 is configured by two adjacent flow path layers 21 adjacent to the respective lead flow path layers 12 on both outer sides of the first flow path portion 10 in the stacking direction Z. As shown in FIGS. 2 and 3, each flow path layer 2 (adjacent flow path layer 21) of the second flow path section 20 has a flow path width W, a flow path height (thickness) H 2, and a flow path length L. And have substantially the same shape. The channel height H2 of the adjacent channel layer 21 is smaller than the channel height H1 of each channel layer 2 of the first channel unit 10.

  As shown in FIG. 3, each adjacent flow path layer 21 includes an inlet 21a at one end on the X1 direction side and an outlet 21b at the other end on the X2 direction side. The adjacent channel layer 21 has a channel opened to the outside at an inlet 21a at one end and an outlet 21b at the other end, and an outer peripheral portion excluding the inlet 21a and the outlet 21b is closed by a side bar 4 (see FIG. 2). Yes. A header tank or the like (not shown) is attached to each of the inlet 21a and the outlet 21b. The second fluid 8 is supplied from the outside to the inlet 21a through the header tank, and the second fluid 8 after heat exchange is discharged from the outlet 21b through the header tank.

  The tube plate 5 partitions the adjacent channel layer 21 and the outlet channel layer 12 adjacent to the adjacent channel layer 21. As described above, the through hole 15 is not provided in the tube plate 5. A side plate 6 is provided outside the adjacent flow path layer 21.

  The second fluid 8 flowing in the adjacent flow path layer 21 flows in the X2 direction from the inlet 21a at one end (end in the X1 direction) toward the outlet 21b at the other end (end in the X2 direction). In addition, the gas 7a (evaporated first fluid 7) flowing through the outlet flow path layer 12 passes from the through hole 15 at one end (X1 direction end) of the partition member 14 to the outlet 12a at the other end (X2 direction end). In the X2 direction. Therefore, the core 1 of the first embodiment is a parallel flow type core in which the first fluid 7 (gas 7a) and the second fluid 8 flow in the same direction along the X direction. The fluid flow method in the core 1 is a counter flow type in which the first fluid 7 and the second fluid 8 flow in opposite directions, or a cross flow type in which the first fluid 7 and the second fluid 8 intersect. Also good.

(Explanation of the flow of liquefied gas and heat medium)
Next, the flow of the first fluid 7 and the second fluid 8 in the core 1 of the first embodiment will be described.

  As shown in FIG. 3, the first fluid 7 flows in from the inlet 11a of the central introduction flow path layer 11, and flows through the introduction flow path layer 11 in the X2 direction. At this time, the low temperature first fluid 7 in the introduction flow path layer 11 receives heat by heat exchange with the relatively high temperature first fluid 7 flowing in the adjacent intermediate flow path layer 13. The first fluid 7 branches at the other end of the introduction flow path layer 11 and flows into the intermediate flow path layer 13 adjacent to each other through the through holes 15.

  In each intermediate flow path layer 13, the first fluid 7 circulates in the flow direction and flows in the opposite X1 direction. At this time, the first fluid 7 of the intermediate flow path layer 13 receives heat and evaporates by heat exchange with the relatively high-temperature gas 7 a flowing through the adjacent outlet flow path layer 12. In the middle of the intermediate flow path layer 13, the liquid phase first fluid 7 and the gas phase gas 7a are mixed, but in the vicinity of the through-hole 15 at one end (end portion in the X1 direction), the gas phase gas 7a. It has become. The gas 7 a flows into the outlet channel layer 12 adjacent to each other through the through hole 15 at one end of each intermediate channel layer 13.

  In each outlet channel layer 12, the gas 7 a circulates in the X2 direction by turning the circulation direction, and is discharged to the outside from the outlet 12 a at the other end (X2 direction end) of each outlet channel layer 12. On the other hand, the second fluid 8 flows in from the inlet 21a of the adjacent flow path layer 21 adjacent to the outlet flow path layer 12, flows through the adjacent flow path layer 21 in the X2 direction, and is at the other end (end in the X2 direction). It is discharged from the outlet 21b. The gas 7a in the outlet flow path layer 12 receives heat and is heated by heat exchange with the second fluid 8 flowing in the adjacent flow path layer 21 adjacent thereto. As a result, the first fluid 7 supplied to the core 1 in the low-temperature liquid phase is evaporated and heated while meandering in the first flow path portion 10 in the X direction, and becomes a gas phase gas 7a. Discharged.

(Effect of 1st Embodiment)
In the first embodiment, the following effects can be obtained.

  In the first embodiment, as described above, the first flow path portion 10 and the second flow path portion 20 are liquefied by providing them in the laminated core 1 in which a plurality of planar flow path layers 2 are stacked. The gas evaporator 100 can be reduced in size. In addition, since the second flow path portion 20 can be configured by the planar closed flow path layer 2, unlike the open rack type structure in which the fluid is supplied to the outside, it is easily mounted on the moving body. can do. Furthermore, by configuring the first flow path portion 10 to have a folded flow path shape, the first fluid 7 passes through the folded flow path from the introduction flow path layer 11 to the discharge flow path layer 12. In the middle, the temperature of the first fluid 7 gradually approaches the temperature of the second fluid 8 by heat exchange between the first fluids 7 flowing through the adjacent flow path layers 2, and the outside after the temperature of the second fluid 8 is approached. Thus, heat exchange between the first fluid 7 and the second fluid 8 flowing through the second channel portion 20 can be performed in the outlet channel layer 12. As a result, even if the core 1 having a laminated structure is employed, the temperature difference between the first fluid 7 and the second fluid 8 between the adjacent outlet channel layer 12 and the adjacent channel layer 21 can be reduced. As a result, according to the liquefied gas evaporator 100 of the first embodiment, a stacked heat exchanger (liquefied gas evaporation) that is small in size and can suppress a temperature difference between adjacent flow path layers from becoming too large. Device).

  In the first embodiment, as described above, the first fluid 7 is a low temperature side fluid and the second fluid 8 is a high temperature side fluid. And the core 1 is comprised so that the 1st fluid 7 which distribute | circulates the 1st flow-path part 10 may be heated up by heat exchange with the 2nd fluid 8 which distribute | circulates the 2nd flow-path part 20. FIG. Accordingly, the temperature of the first fluid 7 is gradually raised while the first fluid 7 on the low temperature side is folded back in the first flow path portion 10, and the temperature between the first fluid 7 and the second fluid 8 after the temperature rises. Heat exchange. As a result, even when the supply temperature of the first fluid 7 is extremely low, it is possible to suppress the second fluid 8 on the high temperature side from icing and blocking the adjacent flow path layer 21.

  Further, in the first embodiment, as described above, the first fluid 7 that has flowed into the introduction channel layer 11 in the state including the liquid phase is evaporated in the first channel unit 10, so that the first fluid in the gas phase state is evaporated. 7 gas 7a is caused to flow out from the outlet flow path layer 12. Thereby, the liquefied gas evaporator 100 which evaporates the 1st fluid 7 which flows into the introductory flow path layer 11 in a liquid phase state, and flows out from the derivation flow path layer 12 in the state of gas 7a can be comprised. Even in this case, since the temperature difference between the first fluid 7 (liquefied gas) and the second fluid 8 (heat medium) can be suppressed by the first flow path portion 10 having the folded structure, the liquefied gas evaporator 100 can be easily downsized. it can.

  In the first embodiment, as described above, the gas in the gas phase state in which the first fluid 7 evaporates between the introduction flow path layer 11 and the discharge flow path layer 12 flows into the discharge flow path layer 12. In addition, the number of turns of the first flow path unit 10 is set. Thereby, the temperature of the first fluid 7 when flowing into the outlet flow path layer 12 can be reliably increased to the evaporating temperature or higher, so that it is effectively caused by freezing of the second fluid 8 in the adjacent flow path layer 21. Blockage of the flow path can be suppressed.

  In the first embodiment, as described above, the introduction flow path layer 11 is arranged at the center in the stacking direction in the first flow path section 10, and the outlet flow path layer 12 is disposed in the stacking direction in the first flow path section 10. Place each on the outermost of both. And the 1st flow path part 10 is formed in the branched flow path shape branched and folded from the center introduction flow path layer 11, and the 2nd flow path part 20 of the 1st flow path part 10 in the lamination direction is formed. It is comprised by the adjacent flow path layer 21 adjacent to each derivation | leading-out flow path layer 12 on both outer sides. Accordingly, heat exchange between the first fluid 7 and the second fluid 8 can be performed on both sides in the stacking direction, so that the heat transfer area between the first fluid 7 and the second fluid 8 can be increased. Moreover, since the introduction flow path layer 11 through which the first fluid 7 in the coldest state flows can be arranged at the center of the core 1, it is possible to suppress the outer surface temperature of the core 1 from becoming too low.

  Moreover, in 1st Embodiment, as mentioned above, the 1st flow path part 10 is formed in the flow path shape folded over several flow path layers 2 via the through-hole 15 of the partition member 14a (14b). To do. Thereby, the flow path shape turned up inside the 1st flow path part 10 (core 1) is realizable. As a result, for example, the liquefied gas evaporator 100 can be reduced in size compared to a structure in which the first fluid 7 is drawn out from one flow path layer 2 and introduced into another flow path layer 2. . Further, when the first fluid 7 is drawn to the outside, unlike the possibility that the outer surface of the drawn flow path portion becomes too low in temperature, the liquefied gas evaporator 100 of the first embodiment has the core 1 The outer surface temperature can be suppressed from becoming too low. That is, in 1st Embodiment, it can suppress that the outer surface of the core 1 freezes.

  Moreover, in 1st Embodiment, as mentioned above, the 1st flow path part 10 and the 2nd flow path part 20 are comprised with the material whose heat conductivity is 50 W / (mxK) or less. Thereby, the heat conductivity of the 1st flow path part 10 and the 2nd flow path part 20 becomes low compared with the material of high heat conductivity like aluminum (about 195 W / m * K), for example. Therefore, the flow path surface temperature (surface temperature of the tube plate 5) on the side of the adjacent flow path layer 21 adjacent to the outlet flow path layer 12 through which the first fluid 7 flows is excessively deviated from the temperature of the second fluid 8. Can be suppressed. That is, since it can suppress that the flow path surface temperature on the adjacent flow path layer 21 side falls too much, the freezing of the 2nd fluid 8 in the adjacent flow path layer 21 can be suppressed easily.

(Explanation of simulation results)
Next, with reference to FIG. 4, the simulation result performed in order to confirm the effect of the liquefied gas evaporator 100 by 1st Embodiment is demonstrated. In the simulation, oxygen (liquid oxygen, boiling point of about −190 ° C.) was adopted as the first fluid 7, and water was adopted as the second fluid 8, and the respective temperature distributions while passing through the liquefied gas evaporator 100 were calculated.

  FIG. 4 is a diagram showing a simulation result, and shows an outline of a temperature distribution with shades (hatching) in which a temperature range is divided into six stages in a flow path portion. The inlet temperature T1 of the first fluid 7 (liquid oxygen) at the inlet 11a of the introduction flow path layer 11 was set to -190 ° C. The inlet temperature T5 of the second fluid 8 (water) at the inlet 21a of the adjacent flow path layer 21 was set to 25 ° C.

  Since the first fluid 7 flows into the introduction flow path layer 11 at a temperature substantially equal to the boiling point, evaporation proceeds while traveling through the introduction flow path layer 11 in the X2 direction. Since the temperature is substantially constant during evaporation, the temperature T2 of the first fluid 7 slightly increases at the other end (X2 side end) of the introduction flow path layer 11, but is substantially equal to the inlet temperature T1 (T2≈− 190 ° C.), and the gasification rate of the first fluid 7 was about 60%. At one end (X1 side end) of the intermediate flow path layer 13, the gasification rate of the first fluid 7 was about 100%, and the temperature T3 of the first fluid 7 (gas 7a) rose to about −100 ° C. In the outlet channel layer 12, the temperature of the gas 7a rose from one end to the outlet 12a at the other end, and reached about 0 ° C. at the outlet temperature T4.

  The second fluid 8 flows in from the inlet 21a of the adjacent flow path layer 21 at the inlet temperature T5 = 25 ° C., decreases in temperature while reaching the outlet 21b at the other end (X2 direction end), and is about the outlet temperature T6. It became 15 degreeC.

  As a result, according to the liquefied gas evaporator 100 of the first embodiment, the temperature of the first fluid 7 when flowing into the outlet flow path layer 12 is changed from −190 ° C. (T1) to about −100 ° C. (T3). It was confirmed that the temperature difference between the outlet channel layer 12 and the adjacent channel layer 21 adjacent to each other can be suppressed from becoming too large. As a result, it was confirmed that a sudden temperature drop of the second fluid 8 in the adjacent channel layer 21 can be suppressed, and the channel blockage due to freezing of the second fluid 8 can be suppressed.

[Second Embodiment]
Next, a second embodiment of the present invention will be described with reference to FIG. In the second embodiment, unlike the first embodiment in which the liquefied gas evaporator 100 is shown in which a low-temperature liquefied gas is evaporated by heat exchange with a heat medium and supplied as a gas phase gas, the evaporator is An example of a different heat exchanger 200 will be described.

(Configuration of Second Embodiment)
The heat exchanger 200 of the second embodiment is structurally similar to the liquefied gas evaporator 100 of the first embodiment. Therefore, for each part of the heat exchanger 200, the same reference numerals as those of the first embodiment are used, and the description of the structure is omitted.

  In the second embodiment, the first fluid 71 flows through the first flow path unit 10, and the second fluid 81 flows through the second flow path unit 20.

  The first fluid 71 is a low temperature side fluid, for example, a cryogenic gas. The gas is, for example, oxygen, nitrogen, hydrogen or the like, and flows into the introduction flow path layer 11 from the inlet 11a in a cryogenic gas phase state. The second fluid 81 is a high temperature side fluid and a heat medium. As the heat medium, water, seawater, air, or the like may be used as in the first embodiment, or other fluids may be used. The second fluid 81 flows into the adjacent flow path layer 21 at room temperature equivalent to the external environment, for example.

  The core 1 is configured to raise the temperature of the first fluid 71 in a gas phase that circulates through the first flow path 10 by heat exchange with the second fluid 81 that flows through the second flow path 20. . The first fluid 71 is exchanged with the second fluid 81 by heat exchange between the first fluids 71 in the process of turning back (intermediate channel layer 13) while flowing from the inlet channel layer 11 to the outlet channel layer 12. Reduce the temperature difference. As a result of heat exchange between the lead-out flow path layer 12 and the adjacent flow path layer 21, the first fluid 71 is heated by the heat contained in the second fluid 81, and remains in a gas phase at a predetermined outlet temperature. To be supplied.

  Other configurations of the second embodiment are the same as those of the first embodiment.

(Effect of 2nd Embodiment)
Also in the second embodiment, similarly to the first embodiment, the temperature of the first fluid 71 is gradually increased while the first fluid 71 passes through the folded flow path, although it has a laminated structure. A temperature of 81 can be approached. Thereby, it is possible to provide a stacked heat exchanger 200 that is small in size and capable of suppressing the temperature difference between the adjacent outlet channel layer 12 and the adjacent channel layer 21 from becoming too large.

  In the second embodiment, unlike the liquefied gas evaporator 100 of the first embodiment, the heat exchanger 200 is configured as a temperature raising device for the first fluid 71 that does not involve phase change (evaporation) of the first fluid 71. However, even in this case, it is possible to prevent the adjacent flow path layer 21 from being blocked due to freezing of the second fluid 81 on the high temperature side due to heat exchange with the cryogenic first fluid 71.

[Third Embodiment]
Next, a third embodiment of the present invention will be described with reference to FIG. In the third embodiment, the first embodiment showing the liquefied gas evaporator 100 that evaporates the first fluid 7 and the second embodiment showing the heat exchanger 200 that raises the temperature of the first fluid 71. In contrast, an example of the heat exchanger 300 that recovers the heat of the high-temperature first fluid 72 will be described.

(Configuration of Third Embodiment)
The heat exchanger 300 of the third embodiment is structurally similar to the liquefied gas evaporator 100 of the first embodiment and the heat exchanger 200 of the second embodiment. Therefore, the same reference numerals as those of the first and second embodiments are used for the respective parts of the heat exchanger 300, and the description of the structure is omitted.

  In the third embodiment, the first fluid 72 flows through the first flow path unit 10, and the second fluid 82 flows through the second flow path unit 20.

  The first fluid 72 is a high temperature side fluid and is a high temperature gas or liquid. For example, the first fluid 72 is a reformed gas derived from natural gas (a high-temperature gas discharged from the reformer) or a combustion gas, and flows into the introduction channel layer 11 from the inlet 11a in a high-temperature state. . The second fluid 82 is a low temperature side fluid and a heat medium. As the heat medium, water, air, or the like may be used as in the first embodiment, or other fluids may be used. For example, the second fluid 82 flows into the adjacent flow path layer 21 at room temperature equivalent to the external environment.

  The core 1 is configured to cool the first fluid 72 flowing through the first flow path portion 10 by heat exchange with the second fluid 82 flowing through the second flow path portion 20. The heat of the first fluid 72 is recovered by the second fluid 82, and the second fluid 82 is heated or evaporated. The first fluid 72 is exchanged with the second fluid 82 by heat exchange between the first fluids 72 in the process of turning back (intermediate channel layer 13) while flowing from the inlet channel layer 11 to the outlet channel layer 12. Reduce the temperature difference. As a result of the heat exchange between the outlet channel layer 12 and the adjacent channel layer 21, the first fluid 72 cooled to a predetermined outlet temperature is supplied from the outlet channel layer 12 to the outside and reaches a predetermined outlet temperature. The heated second fluid 82 is supplied to the outside from the adjacent flow path layer 21.

  Other configurations of the third embodiment are the same as those of the first embodiment.

(Effect of the third embodiment)
Also in the third embodiment, as in the first embodiment, the temperature of the first fluid 72 is gradually increased while the first fluid 72 passes through the folded flow path, although it has a laminated structure. 82 can be approached. As a result, it is possible to provide a stacked heat exchanger 300 that is small in size and can suppress the temperature difference between the adjacent outlet channel layer 12 and the adjacent channel layer 21 from becoming too large.

  Further, in the third embodiment, unlike the liquefied gas evaporator 100 of the first embodiment and the heat exchanger 200 of the second embodiment, a heat recovery device (or a cooling device) that recovers the heat of the high-temperature first fluid 72. ), The heat exchanger 300 was configured. In this case, the temperature difference between the outlet channel layer 12 through which the high temperature first fluid 72 flows and the adjacent channel layer 21 through which the second fluid on the low temperature side flows becomes too large. Generation of large thermal stress can be suppressed. As a result, it is possible to reduce the size of the heat exchanger 300 by reducing constraints such as strength design.

[Modification]
The embodiment disclosed this time should be considered as illustrative in all points and not restrictive. The scope of the present invention is shown not by the above description of the embodiment but by the scope of claims for patent, and further includes all modifications (modifications) within the meaning and scope equivalent to the scope of claims for patent.

  For example, in the first to third embodiments, the example in which the plate fin type core 1 is provided as an example of the laminated structure is shown, but the present invention is not limited to this. In the present invention, a diffusion bonding type core may be used in which a flow path layer made of a metal plate in which flow paths are integrally formed is laminated and each flow path layer is bonded by diffusion bonding. Also, a plate-type core in which corrugated metal plates with flow paths integrally formed on the front and back surfaces are laminated, and each flow path layer is joined by sealing or welding to constitute a flow path layer between the metal plates. Also good.

  In the first to third embodiments, in the first channel portion 10, one intermediate channel layer 13 is provided between the inlet channel layer 11 and the outlet channel layer 12, and the channel is folded twice. Although an example configured as described above is shown, the present invention is not limited to this. In the present invention, the first flow path portion may have a flow path shape that turns back a number other than twice.

  In the first embodiment, the example of the liquefied gas evaporator 100 including one core 1 including the first flow path unit 10 and the second flow path unit 20 is shown. However, the present invention is not limited to this. I can't. In the present invention, a plurality of cores 1 may be laminated as in the liquefied gas evaporator 100a of the first modification shown in FIG. In this case, as shown in FIG. 7, the second flow path portion 20 (adjacent flow path layer 21) between the plurality of cores 1 is preferably shared. The same configuration can be adopted for the heat exchanger 200 of the second embodiment and the heat exchanger 300 of the third embodiment. The liquefied gas evaporator 100a is an example of the “heat exchanger” in the present invention.

  Moreover, in the said 1st Embodiment, the partition member 14 (14a, 14b) which has the through-hole 15 was provided, and the 1st flow path part 10 showed the example comprised so that a flow path might be turned up inside the core 1. However, the present invention is not limited to this. In the present invention, like the liquefied gas evaporator 100b of the second modification shown in FIG. 8, the first flow path unit 110 may be configured to fold the flow path outside the core 1. In the first flow path portion 110 according to the second modification, each flow path layer is partitioned by the tube plate 5 without the through hole 15. An opening 111 is provided at the other end (X2 direction end) of the introduction flow path layer 11 and the intermediate flow path layer 13 in the first flow path portion 110, and the three openings 111 are the header portions 112. Are covered so as to communicate with each other. Similarly, an opening 111 provided at one end (end in the X1 direction) of the intermediate flow path layer 13 and the outlet flow path layer 12 is covered by the header section 112 so as to communicate with each other. Thus, the flow path of the first flow path part 110 is folded outside the core 1 by the header part 112. The same configuration can be adopted for the heat exchanger 200 of the second embodiment and the heat exchanger 300 of the third embodiment. The liquefied gas evaporator 100b is an example of the “heat exchanger” in the present invention.

  Further, in the first embodiment, the gas phase gas 7 a obtained by evaporating the first fluid 7 from the introduction flow path layer 11 to the discharge flow path layer 12 flows into the discharge flow path layer 12. Although the example which comprised 1 flow path part 10 was shown, this invention is not limited to this. In the present invention, the gas flowing into the lead-out flow path layer may contain a part of the liquefied gas that remains in the liquid phase. Even in this case, an effect of suppressing freezing of the heat medium in the second flow path portion can be obtained. In this case, for example, it may be possible to prevent icing by providing an auxiliary electric heater outside the second flow path.

  Moreover, in the said 1st Embodiment, the example which provided the 1st flow path part 10 which has the branched flow path shape branched and turned from the center introduction flow path layer 11 to the two intermediate flow path layers 13 was shown. However, the present invention is not limited to this. In the present invention, for example, the first flow path portion is formed so that the flow path shape is folded without branching from the introduction flow path layer at the lower end in the stacking direction toward the lead-out flow path layer at the upper end in the stacking direction. It may be configured. In this case, since the introduction channel layer through which the low-temperature liquefied gas flows is disposed at the outermost part (lower end) of the core, it is preferable to provide a heat insulating material or the like on the lower surface side of the core.

1 core (heat exchanger)
2 Channel layer 7 First fluid (low temperature side fluid, liquefied gas)
8 Second fluid (high temperature side fluid, heat medium)
10, 110 1st channel part (liquefied gas channel part)
DESCRIPTION OF SYMBOLS 11 Introduction flow path layer 11a Inlet 12 Outlet flow path layer 12a Outlet 14 Partition member 15 Through-hole 20 2nd flow path part (heat-medium flow path part)
21 Adjacent channel layer 71 1st fluid (low temperature side fluid)
72 1st fluid 81 2nd fluid (high temperature side fluid)
82 Second fluid 100, 100a, 100b Liquefied gas evaporator (heat exchanger)
200, 300 Heat exchanger Z Stacking direction

Claims (8)

It has a laminated structure in which a plurality of planar flow path layers are stacked, and includes a heat exchange section including a first flow path section for flowing a first fluid and a second flow path section for flowing a second fluid,
The channel layer of the first channel part includes an introduction channel layer having an inlet and an outer outlet channel layer having an outlet, and the first channel part has a folded channel shape. Have
The flow channel layer of the second flow channel unit includes the adjacent flow channel layer adjacent to the outlet flow channel layer of the first flow channel unit outside the first flow channel unit. The first fluid is a low temperature side fluid;
The second fluid is a high temperature side fluid,
The heat exchanging unit is configured to raise the temperature of the first fluid flowing through the first flow path unit by heat exchange with the second fluid flowing through the second flow path unit. Item 2. The heat exchanger according to Item 1.   The first flow path portion evaporates the first fluid that has flowed into the introduction flow path layer in a state including a liquid phase, and causes the gas of the first fluid in a gas phase state to flow out from the outlet flow path layer. The heat exchanger according to claim 2, which is configured as follows.   The number of times the first flow path portion is folded is set so that gas in a vapor phase obtained by evaporating the first fluid flows into the discharge flow path layer from the introduction flow path layer to the discharge flow path layer. The heat exchanger according to claim 3, wherein The introduction channel layer is disposed at the center in the stacking direction in the first channel unit,
The lead-out flow path layers are respectively disposed on both outermost sides in the stacking direction in the first flow path portion,
The first flow path portion has a branched flow path shape branched and folded from the central introduction flow path layer,
The said 2nd flow-path part is comprised by the said adjacent flow path layer adjacent to each said derivation | leading-out flow path layer on the both outer sides of the said 1st flow-path part in the lamination direction. The heat exchanger according to item 1. The first flow path portion further includes a partition member that partitions each of the stacked flow path layers and has a through hole penetrating in the stacking direction,
The heat exchanger according to any one of claims 1 to 5, wherein the first flow path portion has a flow path shape that is folded over a plurality of the flow path layers via the through holes of the partition member. .   The heat exchange according to any one of claims 1 to 6, wherein the first flow path part and the second flow path part are made of a material having a thermal conductivity of 50 W / (mxK) or less. vessel. It has a laminated structure in which a plurality of planar flow path layers are stacked, and includes a heat exchange section that includes a liquefied gas flow path section that circulates liquefied gas and a heat medium flow path section that circulates a heat medium,
The channel layer of the liquefied gas channel section includes an inlet channel layer having an inlet and an outer outlet channel layer having an outlet, and the liquefied gas channel section has a folded channel shape. Have
The liquefied gas evaporator, wherein the flow path layer of the heat medium flow path section includes the adjacent flow path layer adjacent to the outlet flow path layer of the liquefied gas flow path section outside the liquefied gas flow path section.

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