JPH05141892A - Heat exchanger - Google Patents

Abstract

PURPOSE:To prevent fatigue, breakdown of a tube plate by preventing a large temperature difference between both surfaces of the plate at the time of introducing fluid into a heat exchanging chamber. CONSTITUTION:The heat exchanger comprises a lower tube plate 14 for partitioning a heat exchanging chamber 15 and a sea water outlet chamber 20, and a partition plate 34 provided to an inlet nozzle 30 for introducing fluid such as LNG, etc., in the chamber 14. Direct contact of the fluid such as LNG, etc., to be introduced from the nozzle 30 with a lower tube plate 14 is prevented by the plate 34.

Description

Detailed Description of the Invention

[0001]

The present invention relates to liquefied natural gas (hereinafter,
The present invention relates to a tubular heat exchanger used for vaporizing LNG).

[0002]

2. Description of the Related Art Conventionally, as a tube heat exchanger, a fixed tube plate type in which both ends of a linear heat exchange tube are fixed to tube plates, U
Known are a U-tube type in which both ends of a bent tube are fixed to the same tube sheet, and a floating head type in which one head is movable in the axial direction of the tube with respect to the other head. There is. Of these, an example of the horizontal U-tube heat exchanger is shown in FIG.

In the figure, one end of a horizontally extending barrel 100 is closed, and a tube sheet 102 is fixed to the other end.
A heat exchange chamber 103 is formed by the tube sheet 102 and the body 100. An outer plate 104 is disposed at a position opposite to the body 100 with the tube plate 102 as a boundary, and a high-temperature fluid such as seawater (heat that is partitioned by a partition plate 106) between the outer plate 104 and the tube plate 102. An exchange medium) inlet chamber 108 and a hot fluid outlet chamber 110 are formed, and the hot fluid inlet chamber 10
8 is a high temperature fluid inlet nozzle 112,
Each 10 is provided with a hot fluid outlet nozzle 114.

A U-shaped tube 116 bent in a U-shape is provided in the heat exchange chamber 103, and both ends of the U-shaped tube 116 are fixed to the same tube plate 102.
The interior of 6 is in communication with the inside of the high temperature fluid inlet chamber 108 and the inside of the high temperature fluid outlet chamber 110, respectively. A plurality of baffle plates 118 are provided in the heat exchange chamber tube 103, and these are supported by the tube sheet 102 and the body 100 side via a common tie rod 117. An inlet nozzle 121 for a fluid to be heated or cooled (here, a low-temperature fluid such as LNG) is provided at the lower end position of the heat exchange chamber 103, and an outlet nozzle 122 for the vaporized fluid is provided at the upper end position. Is provided.

In such a structure, the U-shaped tube 1 passes through the hot fluid inlet nozzle 112 and the hot fluid inlet chamber 108.
In the state where a high temperature fluid such as seawater is introduced into 16, a low temperature fluid such as LNG is introduced from the inlet nozzle 121, and the above U
The heat exchange with the high temperature fluid inside the character tube 116 causes the vaporized low temperature fluid to be discharged from the outlet nozzle 122.

[0006]

In the above heat exchanger, the heat exchange chamber 103 into which the low temperature fluid is introduced and the high temperature fluid chambers 110 and 108 into which the high temperature fluid is introduced are only separated by the tube sheet 102. Therefore, a large temperature difference occurs on both front and back surfaces of the tube sheet 102. In particular, at the time of cool down for avoiding macroscopic thermal stress, that is, at the time of precooling the heat exchanger by introducing a small amount of LNG into the heat exchange chamber 103 before the start of operation or at the start of operation, etc. A temperature difference occurs, and the bending stress generated in the tube sheet 102 due to the temperature difference may cause fatigue failure in the tube sheet 102. Such a phenomenon becomes more prominent when the temperature difference between the low temperature fluid and the high temperature fluid is large and there is a phase change such as evaporation / boiling or condensation in the heat exchange chamber 103.

Explaining the mechanism of this temperature difference, first, in a state where the tube sheet 102 is not cooled at all, that is, in the initial state where the tube sheet 102 is equal to the high temperature fluid temperature,
When a small amount of cryogenic fluid is put into the heat exchange chamber 103, the cryogenic fluid boils by coming into direct contact with the U-tube 116 and the tube plate 102. Here, the cryogenic fluid and the U-shaped pipe 11
6 and film boiling occurs in the initial stage where the temperature difference between the wall of the tube sheet 102 and the wall of the tube sheet 102 is large, and thereafter, nucleate boiling shifts as the wall temperature decreases. The heat transfer coefficient in this nucleate boiling is h _NB , the wall temperature is T _W , and the saturation temperature of the cryogenic fluid is T _LS.
Then, the amount of heat transfer per unit area, that is, the heat flux q is represented by q = h _NB · (T _W −T _LS ), but the heat transfer coefficient h _NB in this nucleate boiling is in a complete gas phase or liquid layer. It is a very large value as compared with the heat transfer coefficient, and therefore the heat flux q is also very large. Therefore, the evaporation of the low temperature fluid rapidly removes heat from the surface of the tube sheet 102, resulting in a significant decrease in the surface temperature. Becomes Moreover, the cold heat on this surface is infinitely fast.
2 cannot pass through, and in fact, the surface of the tube sheet 102 on the side facing the high temperature fluid chambers 108 and 110 maintains a temperature equal to that of the high temperature fluid for a while even after the temperature of the surface starts to decrease. Therefore, a significant temperature difference occurs on both surfaces before the tube sheet 102 reaches a temperature equilibrium state.

This phenomenon will be described in more detail with reference to FIG. In FIG. 11A, for convenience, the heat exchange chamber 103 is shown on the upper side and the high temperature fluid inlet chamber 108 is shown on the lower side.

First, in the initial state in which the low temperature fluid is not introduced, the surface temperature Tss of the tube sheet 102 facing the heat exchange chamber 103 side and the surface temperature Tcs of the tube sheet 102 facing the high temperature fluid outlet chamber 108 are both initial temperatures (high temperature fluid temperature). ) To. From this state, when the low temperature fluid comes into contact with the tube sheet 102 and evaporates, the surface temperature on the heat exchange chamber 103 side drops sharply to the temperature Tss ₁ , and the temperature difference ΔT with the surface on the high temperature fluid inlet chamber 108 side. ₁ occurs. Moreover, since it takes time for this cold heat to be transferred to the surface on the high temperature fluid inlet chamber 108 side, the surface temperature on the heat exchange chamber 103 side further decreases to temperature Tss ₂ during that time, and the maximum surface temperature difference is reached. The value is ΔT ₂ (>
ΔT ₁ ) is reached.

After the cold heat is transferred to the surface on the high temperature fluid inlet chamber 108 side, the temperature difference between the two surfaces gradually decreases, and finally reaches a steady state as shown in FIG. 11 (b).

Therefore, in such a conventional heat exchanger,
Even if the tube sheet 102 is designed to withstand the thermal stress caused by the surface temperature difference in the steady state (state during continuous operation etc.) as shown in FIG.
Alternatively, immediately after the cooldown ends and the formal operation starts, a surface temperature difference larger than the surface temperature difference in the steady state is generated, and due to this, a large thermal stress is repeatedly generated. Fatigue may occur, causing damage such as cracks. In particular, when the pressure difference between the low temperature fluid and the high temperature fluid is large, the thickness dimension δ of the tube sheet 102 must be set to a large value, which further aggravates the inconvenience. For example, the tube sheet 1
When 02 is formed of stainless steel and the thickness dimension δ is set to 55 mm, it takes about from the time when nucleate boiling occurs on the surface on the heat exchange chamber 103 side to the time when the surface on the high temperature fluid inlet chamber 108 side starts to decrease in temperature. It takes 1 minute, during which a very large surface temperature difference occurs.

Further, such inconvenience similarly occurs when the high temperature fluid is introduced into the heat exchange chamber side and the low temperature fluid is flown into the tube side.

In view of such circumstances, the present invention prevents a large temperature difference between the two surfaces of the tube sheet when the fluid is introduced into the heat exchange chamber, thereby preventing fatigue and breakage of the tube sheet. It aims at providing the heat exchanger which can be prevented.

[0014]

According to the present invention, a heat exchange chamber having an inlet portion into which a fluid to be heated or cooled is introduced and an outlet portion from which the fluid is discharged, and heat exchange with the fluid. A heat exchange medium chamber containing a heat exchange medium, a tube plate partitioning the heat exchange chamber and the heat exchange medium chamber, and provided in the heat exchange chamber, the interior is in communication with the heat exchange medium chamber A heat exchanger comprising a tube having an end fixed to the tube sheet, in which heat is exchanged between a heat exchange medium flowing in the tube and a substance in the heat exchange chamber, and the inlet in the heat exchange chamber. A separator is provided at a position between the section and the tube sheet (Claim 1).

Further, a flow passage for a fluid introduced into the heat exchange chamber is formed in the separator (claim 2), or a part of the separator is brought into contact with the tube plate (claim). By 3), more excellent effects as described later can be obtained.

[0016]

According to the above construction, since the separator is arranged between the inlet and the tube sheet in the heat exchange chamber, the fluid introduced from the inlet does not suddenly come into contact with the tube sheet. , This fluid is received by the separator. Therefore, the temperature change of the surface of the tube sheet facing the heat exchange chamber is gentler than when the separator is not provided, that is, when the fluid comes into direct contact with the tube sheet. The maximum value of the temperature difference between the exchange chamber side surface and the heat exchange medium chamber side surface becomes smaller.

Further, according to the second or third aspect of the invention, a part of the fluid leaked from the flow passage of the separator comes into contact with the tube plate, or the separator itself comes into contact with the tube plate. This promotes heat exchange between the fluid and the tube sheet.

[0018]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A first embodiment of the present invention will be described with reference to FIGS. In this embodiment, a vertical heat exchanger for heating and vaporizing LNG with seawater which is a heat exchange medium will be described, but in the present invention, regardless of the type of fluid or heat exchange medium to be heated or cooled. For example, it can be applied to a heat exchanger for cooling a high temperature fluid with a low temperature fluid which is a heat exchange medium.

The heat exchanger according to this embodiment is provided with a cylindrical body 10 extending vertically as shown in FIG.
The upper tube plate 12 and the lower tube plate 14 are fixed to the upper and lower parts of the upper part, and a heat exchange chamber 15 is formed by these.
A seawater inlet chamber 16 is provided above the upper tube sheet 12, a seawater inlet nozzle 18 is connected to the seawater inlet chamber 16, and a seawater outlet chamber 20 is provided below the lower tube sheet 12. A seawater outlet nozzle 22 and a seawater drain valve 24 are connected to the seawater outlet chamber 20.

A large number of vertically extending tubes 26 are arranged in the heat exchange chamber 15. The upper and lower ends of each tube 26 are fixed to the upper and lower tube plates 12 and 14, respectively.
The inside of 6 is in communication with the inside of the seawater inlet chamber 16 and the inside of the seawater outlet chamber 20, respectively. Further, the body 10 is provided with means (not shown) for absorbing the expansion / contraction difference due to the temperature difference between the body 10 and the pipe 26. Horizontal baffle plates 32 are provided in the heat exchange chamber 15 in a multi-tiered manner in the vertical direction.
A zigzag-shaped LNG passage is formed in the inside 5. Further, an inlet nozzle (inlet portion) 30 for introducing LNG is connected to a lower portion of the heat exchange chamber 15, and an outlet nozzle (outlet portion) 31 for discharging vaporized NG is connected to an upper portion thereof. ..

Further, as a feature of this heat exchanger, the lower tube sheet 14 is located below the inlet nozzle 30.
A separator plate 34, which is thinner than the tube plates 12 and 14, is disposed at a position above the tube plates 12 and 14. The separator 34 is provided over substantially the entire horizontal direction of the heat exchange chamber 15,
As shown in FIG. 2, a through hole 36 for passing the pipe 26 is provided at an appropriate position, and a minute gap is secured between the inner peripheral surface of the through hole 36 and the outer peripheral surface of the pipe 26. There is.

Regarding the attachment of the isolation plate 34, the peripheral edge of the isolation plate 34 may be connected to the inner peripheral surface of the body 10 by welding or the like, but as shown in FIGS. Torso 1
The mounting ring plate 38 is fixed to the inner peripheral surface of the pin 0, and the pin 40 is projected on the upper surface of the mounting ring plate 38, while the separating plate 34
If a long hole 42 extending in the radial direction is provided at the peripheral edge of the separator, and the pin 40 is inserted into the long hole 42, the peripheral edge of the separator plate 34 is placed in the mounting ring plate 38. Since the separating plate 34 can freely expand and contract in the radial direction, it becomes possible to prevent a large thermal stress from being generated in the separating plate 34.

The material of the separator 34 may be set appropriately according to the application, and the thickness dimension may be set small within a range that does not cause a problem in strength. For example, in the case of the LNG vaporization heat exchanger as in this embodiment, the separator 34 is preferably a stainless steel plate having a thickness of about 2 to 3 mm. Also,
The distance between the separating plate 34 and the lower tube plate 14 may be set appropriately according to the structure of the entire heat exchanger.

Next, the operation of the heat exchanger will be described with reference to FIGS.

First, before starting full-scale operation, cool down, that is, in order to avoid macroscopic thermal stress,
A work of precooling the heat exchanger is performed by introducing a small amount of LNG from the inlet nozzle 30 while flowing seawater into the pipe 26.
The LNG introduced during this cooldown is not directly contacted with the lower tube sheet 14, but is once received by the separator 34 as shown in FIG. The LNG 44 shown in the figure is
Boiling on the surface of the tube 26, the vaporized NG (arrow A1) rises without contact with the lower tube sheet 14.

On the other hand, a part of the LNG 44 includes the pipe 26
Passing through the outer peripheral surface of the through hole 36 and the inner peripheral surface of the through hole 36, and descending along the pipe 26, but most of it evaporates on the surface of the pipe 26 during the descending, so that the surface of the lower tube sheet 14 LN to reach
G44 is very small, if any. Therefore, the temperature drop on the surface of the lower tube sheet 14 on the heat exchange chamber 15 side (upper surface in the example in the figure) is much gentler than that of the conventional heat exchanger, and a large surface temperature difference does not occur on the tube sheet 14. .. That is, when the LNG 44 reaches the upper surface of the tube sheet 14, the temperature of the upper surface is lowered and a surface temperature difference ΔT ₁ ′ between the lower surface and the lower surface is generated, so that cold heat is transferred to the lower surface of the tube sheet 14. The maximum surface temperature difference ΔT ₂ ′ occurs until the temperature is changed. This surface temperature difference ΔT ₂ ′ is as shown in FIG.
It is very small compared to the maximum surface temperature difference ΔT ₂ in the conventional heat exchanger shown in (4), so that large thermal stress is prevented from occurring in the lower tube sheet 14. The effect of suppressing the thermal stress can be similarly obtained when a large amount of LNG 44 is introduced at once at the start of full-scale operation after the cool down.

Precooling proceeds in this way, and the lower tube sheet 14
When the space temperature between the separator and the separator 34 drops, the pipe 2
The amount of liquid reaching the upper surface of the lower tube sheet 14 through 6 gradually increases, but since the upper surface temperature Tss of the lower tube sheet 14 has already dropped sufficiently at this time, an excessive temperature difference is generated. And no thermal stress is generated.

Note that, due to the provision of the isolation plate 34 as described above, the cooling rate of the lower tube sheet 14 at the time of cool down decreases, and the lower tube sheet 14 is completely pre-cooled. However, since the time for precooling the entire heat exchanger is relatively long in general, the lower tube sheet 1 is longer than the time required for precooling the entire heat exchanger.
The time required for precooling 4 is seldom longer and therefore there is no risk of adversely affecting the operating efficiency of the heat exchanger.

Further, in this embodiment, LN which is a low temperature liquid is used.
Although the cool down for supplying G44 has been described, in the cool down for introducing the low temperature steam, the heat conduction of the tube 26 is used to cool the tube sheets 12 and 14 without flowing a high temperature fluid such as seawater. Good.

Further, in this embodiment, a gap serving as a flow passage for the LNG 44 is secured between the outer peripheral surface of the pipe 26 and the outer peripheral surface of the through hole 36, but this gap may be eliminated. However, if a part of the LNG 44 is brought into contact with the lower tube sheet 14 by such a gap, the time required for precooling the lower tube sheet 14 can be shortened by that amount, and at the time of use, a separator plate is used. Since the LNG 44 can be filled between the lower tube sheet 14 and the lower tube sheet 14, it is possible to reduce the load on the separator 34 for supporting the LNG 44 in the heat exchange chamber 15.

Next, a second embodiment will be described with reference to FIG. This embodiment is an example in which the present invention is applied to a U-tube heat exchanger. That is, the lower tube sheet 1 shown in the figure
A seawater inlet chamber 45 and a seawater outlet chamber 46, which are partitioned from each other by a partition plate 47, are formed below 4, and the seawater inlet chamber 45 has a seawater inlet nozzle 18, and the seawater outlet chamber 46 has a seawater outlet nozzle 22. It is connected. On the other hand, heat exchange room 1
A U-shaped pipe 26 is arranged in the pipe 5 with both ends thereof facing downward, and both ends of the pipe 26 are connected so that the pipe 26 communicates with both the seawater inlet chamber 45 and the seawater outlet chamber 46. The part is fixed to the lower tube sheet 14.

As described above, the present invention can be applied to various tubular heat exchangers such as a fixed tube plate type, a U tube type, and a floating head type, regardless of the specific structure of the entire heat exchanger. ..

A third embodiment is shown in FIG. Here, a sleeve 48 formed by forging, machining or the like is fitted into the through hole 36 provided in the separator 34, and the sleeve 4
A predetermined minute gap is secured between the inner peripheral surface of 8 and the outer peripheral surface of the tube 26.

According to this structure, the sleeve 4 is
With the arrangement of 8, the area where the minute gap is formed, that is, the area where the heating of the fluid is promoted by the direct contact with the tube 26 is expanded more than the thickness dimension of the separator 34, and the area of the liquid is correspondingly increased. The flow amount will be suppressed. Therefore, if the sleeve 48 having various axial dimensions is mounted in the through hole 36, the evaporation degree according to the axial dimension of the sleeve 48 can be obtained, and therefore, a single heat exchange is performed. It becomes possible to process a plurality of types of fluids in a container.

A fourth embodiment is shown in FIG. Here, the corrugated separator plate 34 has a plurality of protruding portions 50 protruding downward.
Is formed, and the lower end of each protrusion 50 is brought into contact with the lower tube sheet 14.

Even in such a structure, the LNG 44 is suppressed or prevented from coming into direct contact with the lower tube sheet 14, so that a large surface temperature difference does not occur in the lower tube sheet 14. Moreover, the amount of heat transfer between the separator plate 34 and the lower tube plate 14 can be freely adjusted by adjusting the contact area between them. Further, in this structure, the LNG4
4 and the lower tube sheet 14 perform heat exchange, so that LN
G44 may leak from the separator 34 to the lower tube sheet 14 side, or may not leak at all. If no leakage is made, the space between the separator plate 34 and the lower tube plate 14 remains as it is even if the operation is started, but since the separator plate 34 is in contact with the lower tube plate 14. , LNG 44 is eventually supported by the lower tube sheet 14.

In this embodiment, the corrugated separator plate 34 is shown. However, other than this shape, if the separator plate 34 has a shape in which a part of the separator plate 34 comes into contact with the lower tube sheet 14, the same as above. The effect is obtained.

A fifth embodiment is shown in FIG. Here, the separator 34 is provided with a large number of tapered through holes 52 having a minute diameter, and a part of the LNG 44 is leaked from the through holes 52 to the lower tube sheet 14 side in a raindrop manner. Here, each through hole 5
The hole diameter of 2 may be adjusted according to the surface tension of the LNG 44, and it is preferable that the next droplet drop after the falling droplet evaporates by contact with the lower tube sheet 14.

Even in such a structure, it is possible to prevent a large amount of LNG 44 from coming into contact with the lower tube sheet 14 at once, as in the conventional heat exchanger without the separator 34. No large surface temperature difference occurs. The temperature of the portion of the lower tube sheet 14 cooled by the falling droplets is reduced because the heat is supplied from the surroundings and the lower portion of the lower tube sheet 14, and a relatively uniform temperature distribution is secured as a whole. Moreover, since cooling of the lower tube sheet 14 is promoted as compared with the heat exchanger shown in the first embodiment, it is effective especially when it is desired to shorten the time required for cooldown.
Also in this embodiment, a gap may or may not be provided between the outer peripheral surface of the pipe 26 and the inner peripheral surface of the through hole 36.

The present invention is not limited to such an embodiment, and the following embodiments can be taken as an example.

(1) In each of the above embodiments, the low temperature fluid introduced into the heat exchange chamber 15 is heated by the high temperature fluid introduced into the pipe 26 to be evaporated. It can also be applied to a heat exchanger in which high temperature steam is introduced from the lower side, which is cooled by a low temperature fluid in a tube and condensed. Also in this case, when the separator is not present, the vapor suddenly comes into contact with the lower tube sheet and condenses on the surface of the lower tube sheet, which causes a rapid temperature rise on the surface. If a separator is provided, the separator temporarily receives the vapor, and after liquefying, it contacts the lower tube sheet, so that it is possible to prevent the tube sheet surface from rapidly increasing in temperature due to latent heat of condensation. Generation of a large surface temperature difference can be prevented.

In the case of a heat exchanger in which steam is introduced into the heat exchange chamber from above, a separator plate is provided below the upper tube sheet, and the upper tube sheet has the same function as described above. It is possible to prevent a rapid temperature rise on the surface.

(2) In each of the above-mentioned embodiments, the vertical type heat exchanger in which the body 10 extends in the vertical direction is shown, but the present invention is similarly applied to the horizontal type heat exchanger in which the body extends in the horizontal direction. can do. Also in this case, the same effect as described above can be obtained by disposing the separator plate in a portion between the fluid inlet portion and the tube sheet.

[0044]

As described above, according to the present invention, the separator is provided between the tube plate for partitioning the heat exchange chamber and the heat exchange medium chamber and the inlet for introducing the fluid into the heat exchange chamber. Since the fluid introduced from the inlet part is prevented from suddenly coming into contact with the tube sheet, compared to the conventional heat exchanger, it prevents a rapid temperature change on the tube sheet surface due to the contact with the fluid. be able to. Therefore, since a large surface temperature difference and large thermal stress due to this do not occur in the tube sheet,
There is an effect that fatigue and breakage of the tube sheet due to such thermal stress can be prevented in advance.

Further, according to the heat exchangers of claims 2 and 3, a part of the fluid leaked from the flow path of the separator is brought into contact with the tube plate, or the separator itself is brought into contact with the tube plate. Thus, heat exchange between the fluid and the tube sheet can be promoted, and the temperature change rate of the tube sheet can be increased.

[Brief description of drawings]

FIG. 1 is an overall configuration diagram of a heat exchanger according to an embodiment of the present invention.

FIG. 2 is a cross-sectional view showing a main part of the heat exchanger.

3 is a sectional view taken along line III-III in FIG.

FIG. 4 is a cross-sectional view showing an evaporation state of LNG in a main part of the heat exchanger.

FIG. 5 is a diagram showing a temperature gradient in a lower tube sheet of the heat exchanger.

FIG. 6 is a sectional view showing a main part of a heat exchanger according to a second embodiment.

FIG. 7 is a sectional view showing a main part of a heat exchanger according to a third embodiment.

FIG. 8 is a sectional view showing a main part of a heat exchanger according to a fourth embodiment.

FIG. 9 is a cross-sectional view showing the main parts of a heat exchanger according to a fifth embodiment.

FIG. 10 is an overall configuration diagram showing an example of a conventional heat exchanger.

11A is a diagram showing a temperature gradient generated in a tube sheet of the heat exchanger during cooldown, and FIG. 11B is a diagram showing a temperature gradient in the tube sheet in a steady state.

[Explanation of symbols]

 10 Body 12 Upper Tube Sheet 14 Lower Tube Sheet 15 Heat Exchange Chamber 20 Seawater Outlet Chamber (Heat Exchange Medium Chamber) 26 Tube 30 Inlet Nozzle (Inlet) 31 Outlet Nozzle (Outlet) 34 Separator 36,52 Through Hole ( (Flow passage)

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Akio Tsukamoto 644-7 Nagasuna, Noguchi-machi, Kakogawa-shi, Hyogo Prefecture (72) Inventor Kazuhiko Kuwahara 2-10-6-W6302 Kita-Aoki, Higashinada-ku, Kobe (72) Inventor Sakura Ichiro Baba 5-45-1 Morito, Nishi-ku, Kobe-shi

Claims (3)

[Claims] 1. A heat exchange chamber having an inlet part into which a fluid to be heated or cooled is introduced and an outlet part from which the fluid is drawn out, and heat containing a heat exchange medium for exchanging heat with the fluid. An exchange medium chamber, a tube plate that separates the heat exchange chamber from the heat exchange medium chamber, and a tube plate that is provided in the heat exchange chamber, and an end portion is fixed to the tube sheet in a state where the inside is in communication with the heat exchange medium chamber. A heat exchanger in which heat is exchanged between a heat exchange medium flowing in the pipe and a substance in the heat exchange chamber, in the heat exchange chamber, between the inlet portion and the tube plate. A heat exchanger characterized in that a separator is provided at the position. 2. The heat exchanger according to claim 1, wherein a flow passage for a fluid introduced into the heat exchange chamber is formed in the separator. 3. The heat exchanger according to claim 1, wherein a part of the separator plate is in contact with the tube plate.