JP2001263965A - Plate fin type heat exchanger - Google Patents

Abstract

(57) [Summary] [PROBLEMS] Even if it is used for an evaporator used for a chemical process such as a fuel cell or a hydrogen production device, or a fuel cell for an automobile or the like which is expected to vibrate or tilt during traveling, heat is generated. Provide a plate fin type heat exchanger with excellent exchange efficiency, light weight and compact configuration. SOLUTION: In a configuration of an orthogonal plate fin type heat exchanger, a header tank for a low-temperature fluid passage is arranged in a length direction of a fluid passage of a high-temperature fluid, and a low-temperature fluid inlet is divided into a primary distribution and a secondary distribution. Divided into two chambers, provided with small holes for distribution in the partition for partitioning, increased the amount of low-temperature fluid distributed from the inlet to each low-temperature fluid passage toward the inlet of the high-temperature fluid passage, and the lower After being introduced from the header tank and exchanging heat and exiting to the lower header tank, it is possible to make a U-turn so that heat is exchanged again with the high temperature fluid at the outlet side of the high temperature fluid passage, so that the evaporator can Unentrained raw fuel is not entrained in the vaporized gas to the fuel reformer.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a heat exchanger for use in a chemical process such as a fuel cell power generator, a hydrogen production apparatus, and the like. The present invention relates to a high-efficiency plate-fin type heat exchanger in which an evaporator is reduced in size and weight and can be applied to portable (movable) applications such as automobiles.

[0002]

2. Description of the Related Art Fuel cell devices using hydrogen for the anode and oxygen or air for the cathode have been developed. In particular, devices that use waste heat and use phosphoric acid or molten carbonate as an electrolyte have been actively developed. Have been. The fuel includes:
Hydrocarbons such as natural gas are reformed and used, and methanol and the like are used.

[0003] This fuel processing system has, for example, a configuration in which natural gas is reformed and hydrogenated by steam and heat produced separately, or a configuration is used in which methanol and water are evaporated. A heat exchanger is important for both the reforming and the evaporation, and is a key to the power generation efficiency of the fuel cell.

[0004]

In a chemical process such as a fuel cell or a hydrogen production apparatus utilizing waste heat such as high-temperature exhaust gas, a liquid which has not been vaporized flows out from the evaporator to the evaporator. When supplied to the catalyst layer of the next reformer, the heat of vaporization is deprived in this part, and the reforming reaction is not effectively performed due to a decrease in temperature. Improvement of heat exchange efficiency is strongly required.

[0005] On the other hand, lightweight and compactness are also required.
In fuel cells used for portable (moving) applications such as automobiles, the heat exchanger used for the above-mentioned reforming and evaporating works efficiently and continuously even if there is vibration or inclination during traveling. It is required to flow down to improve the heat exchange efficiency.

The present invention can be applied to an evaporator or the like used for a chemical process such as a fuel cell or a hydrogen production apparatus, and a heat exchange efficiency even if used for a fuel cell of an automobile or the like in which vibration or inclination during running is assumed. It is an object of the present invention to provide a plate fin type heat exchanger having an excellent lightweight and compact configuration.

[0007]

Means for Solving the Problems The present inventors have developed a fuel evaporator for a fuel cell, for example, with a lightweight and compact structure.
As a result of various investigations aimed at a configuration in which the working fluid flows down efficiently and without interruption even in the case of vibration or inclination of automobiles, etc., in the configuration of an orthogonal plate fin type heat exchanger, a low-temperature fluid It has been found that the objective can be achieved by arranging a header tank for the passage and increasing the distribution amount of the low-temperature fluid from the header tank to each low-temperature fluid passage toward the inlet side of the high-temperature fluid passage.

According to the present invention, a low-temperature fluid passage is arranged in a direction orthogonal to the downflow direction of the high-temperature fluid passage to form a heat exchange section, and upper and lower header tanks for low-temperature fluid are arranged in the downflow direction of the high-temperature fluid passage. In the heat exchanger, a small hole for distribution is provided in the partition wall where the fluid inlet of the upper header tank is divided into two chambers of primary distribution and secondary distribution, and the distribution amount of the low-temperature fluid from the inlet to each low-temperature fluid passage The plate fin type heat exchanger is characterized in that the number is increased toward the inlet side of the high-temperature fluid passage.

[0009]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention is directed to a cross-flow type plate fin type heat exchanger.
The chamber is divided into two chambers, the primary distribution and the secondary distribution, and a small hole for distribution is provided in the partition for partitioning, and the distribution amount of the low-temperature fluid from the inlet to each low-temperature fluid passage is increased toward the inlet of the high-temperature fluid passage. If possible, the heat exchanger may have any configuration.

[0010] In particular, in order to reduce the size and weight and improve the heat exchange efficiency, in the cross-flow type heat exchange section, a low-temperature fluid is introduced from the upper header tank and exchanges heat to the lower header tank. After exiting, the heat exchange efficiency can be further improved by making a U-turn so that heat exchange with the high-temperature fluid can be performed again at the outlet side of the high-temperature fluid passage.

A preferred configuration of the present invention will be described in detail with reference to the drawings. As shown in FIG. 1A, B and FIG. 2A, the high-temperature fluid passage is arranged in the left-right direction of the evaporator,
The low-temperature fluid passages are arranged in the vertical direction perpendicular to the flow direction of H. As shown in FIG. 2B, the heat exchange unit 1 is formed by alternately stacking the high-temperature fluid passages and the low-temperature fluid passages here.

In FIG. 1, an inlet header tank 2 for the high-temperature fluid H is provided on the left side of the heat exchange section 1, and the high-temperature fluid is provided on the right side of the heat exchange section 1.
An outlet header tank 3 for H is provided, and an upper header tank 4 for low-temperature fluid L is disposed above the heat exchange section 1 in a flowing direction of the high-temperature fluid flow path, and a low-temperature fluid L A lower header tank 5 is provided.

[0013] The upper header tank 4 and the heat exchange section 1 have a partition wall 6 arranged in the flow direction of the low temperature fluid in order to divide them in the flow direction of the high temperature fluid. As viewed in the flowing direction of the high-temperature fluid H, the downstream side of the partition 6 of the upper header tank 4 is a low-temperature fluid introduction portion 4a, and the upstream side of the partition 6 is a low-temperature fluid outlet 4b.

[0014] The partition wall of the heat exchange unit 1 when viewed in the flowing direction of the high-temperature fluid H
The downstream side of 6 constitutes an evaporating section 1a for elevating the temperature of the low-temperature fluid L and evaporating it, and the upstream side of the partition 6 constitutes a superheat section 1b for heating the low-temperature fluid again. Lower header tank
Numeral 5 functions as a header tank for turning back the low-temperature fluid, is countercurrent to the high-temperature fluid, and constitutes a manifold that connects both the evaporator 1a and the superheater 1b.

It is preferable that the position of the partition wall 6 in the heat exchange section 1 in the flow direction of the high-temperature fluid is determined by the ratio of the heat transfer area. The heat transfer area of the evaporating section 1a of the heat exchange section 1 is A, and the superheat section 1b is
In the case of B, it is desirable that A / (A + B) is 0.9 or more.

This is because the heat transfer area of the superheat section 1b is appropriately reduced to limit the amount of heat received, the temperature of the outlet side is prevented from rising excessively, and the temperature of the low-temperature fluid rising through the superheat section 1b is reduced. The purpose is to increase the flow velocity and evaporate and evaporate the unvaporized raw fuel in the lower header tank 5 in the superheat section 1b along with the outlet section 4b. The inventors have found that the heat transfer area ratio for achieving this object is A / (A + B) ≦ 0.9.
Was confirmed.

In the introduction portion 4a of the upper header tank 4, a distribution passage 7 composed of an elongated pipe is disposed at the center of the tank as a passage for introducing a low-temperature fluid, with the downstream side of the high-temperature fluid as an inlet. As shown in FIGS. 3 and 4, a large number of distribution small holes 8, 9 are provided downward. Further, the distribution small holes 8, 9 of the distribution passage 7 are provided on the upstream side of the high temperature fluid of the introduction portion 4a, and are provided on the downstream side of the high temperature fluid. That is, the introduction part 4a is divided into two chambers of the primary distribution and the secondary distribution in the pipe-shaped distribution passage 7, and the low-temperature fluid is introduced through the distribution small holes 8, 9 provided in the distribution passage 7. The high-temperature fluid of the portion 4a is distributed so as to flow more on the upstream side and less on the downstream side. Therefore, it is possible to prevent a large amount of low-temperature fluid from being sufficiently heated on the high-temperature fluid inlet header tank 2 side of the heat exchange unit 1 and to prevent insufficient heating on the downstream side of the high-temperature fluid.

As shown in FIG. 4, the distribution small holes 8, 9 are formed in distribution passages.
In the case where the angle between the small holes on both sides as viewed from the cross section of FIG. 7 is wide and narrow, the low temperature fluid can be distributed to all the desired low temperature fluid passages in the introduction portion 4a, and the distribution passage 7 is provided.
In the longitudinal direction, the arrangement pattern of the number of perforations is changed as described above. That is, it is desirable that the distribution small holes 8, 9 are arranged with the hole diameter, the number of holes, and the injection direction changed in accordance with the heat load on the high-temperature fluid passage side.

Although a small-diameter pipe is used here for the distribution passage 7, for example, one or more triangular cylinders, square cylinders, or polygonal cylinders may be used. Can be appropriately selected according to the configuration of the above, required fluid type, heat exchange specification, and the like. Further, the direction of introduction of the low-temperature fluid into the distribution passage 7 may be any of a countercurrent flow and a parallel flow with the high-temperature fluid.

As shown in FIGS. 1B and 2B, the height of the lower header tank 5 is desirably relatively low in order to increase the speed of fluid passing through the tank, and the height h is preferably 20 mm or less. And more preferably 10 mm or less.

In the present invention, it is desirable that the space inside the lower header tank 5 is filled with or inserted with a heat transfer material from the upper heat exchange section to promote evaporation and vaporization. For example, as shown in FIG.2B, when this heat transfer body is a corrugated fin in a low-temperature fluid passage, heat from the upper heat exchange unit 1 is transmitted to the unvaporized raw fuel staying here by the corrugated fin, Evaporation can be promoted.

When the tube plate between the high-temperature fluid passage and the low-temperature fluid passage of the heat exchange unit 1 is configured to protrude into the space in the lower header tank 5, the heat from the upper heat exchange unit is formed by this tube plate. Is transmitted to the unvaporized raw fuel retained here, and it is possible to promote evaporation and vaporization.

With the above configuration, for example, methanol and steam reforming water as raw fuels introduced into the upper header tank 4 as a low-temperature fluid are supplied to the upstream side of the high-temperature fluid at the introduction section 4a by the distribution passage 7, After being distributed so as to flow to the downstream side in a small amount, and after being evaporated and vaporized in the evaporating section 1a, it enters the superheat section 1b through the lower header tank 5 and is heated again.

The unvaporized raw fuel that has entered the lower header tank 5 through the evaporating section 1a is pushed by a mixed gas of vaporized methanol and water, or receives heat transfer from the upper heat exchanging section 1. Into the superheat section 1b, and from the outlet section 4b of the upper header tank 4, the completely vaporized mixed gas of methanol and water exits and is supplied to the next-stage reformer. Become.

[0025]

EXAMPLE 1 In the configuration shown in FIGS. 1 and 2, the size of the heat exchange section was 100 mm.
A distribution passage with an outer diameter of 18 mm is placed in the upper header tank, and the height of the lower header tank is set so that × 100 mm, length 500 mm, and the position of the partition wall are approximately 85 mm from the upstream side of the heat exchange section. Was set to 8 mm, and an evaporator was prepared by brazing using stainless steel for all materials such as a tube plate and a corrugated fin.

COMPARATIVE EXAMPLE 1 In the configuration shown in FIGS. 1 and 2, the heat exchanging section has the same dimensions as Comparative Example 1, and both the upper and lower inlet header tanks and outlet header tanks have a height of 35 mm. An evaporator was prepared in the same manner using stainless steel in all cases without setting a partition wall and providing a distribution passage in the upper header tank.

Comparative Example 2 In the configuration shown in FIG. 1 and FIG. 2, the heat exchange part has the same dimensions as in Example 1, and the position of the partition wall is approximately 85 mm from the upstream side of the heat exchange part. The inlet header tank and the outlet header tank arranged vertically are set at 35 mm height so that they are located, and a stainless steel is used for all evaporators without distributing passages in the upper header tank. did.

Using the evaporator of the present invention and the evaporator of the comparative example, a combustion gas of about 600 ° C. is flowed as a high-temperature fluid, and methanol and water are introduced as low-temperature fluids.
After evaporating and leaving the evaporator, the temperature was measured.

In the structure of Comparative Example 1, the mixed gas temperature of vaporized methanol and water was 185 ° C., and contained a little liquid. In the configuration of Comparative Example 1, the temperature of the mixed gas of vaporized methanol and water was 190 ° C., and contained a slight amount of liquid. On the other hand, in the evaporator of the present invention, the outlet temperature was 195 ° C. and the entire amount was vaporized, and there was no unvaporized component.

[0030]

According to the present invention, the heat exchange section is divided into a low-temperature fluid evaporating section and a superheat section, and the lower header tank is made into a manifold connecting both parts, so that the low-temperature fluid is twice as high as the high-temperature fluid. There is no heat exchange structure.In addition to optimizing the heat transfer area ratio between the evaporator and superheat in the heat exchange section, increasing the flow velocity in the superheat section, and transferring heat from the heat exchange section to the lower header tank With the configuration that makes the heat good, it is possible to improve the heat exchange efficiency, and it is possible to reduce the size of the heat exchanger.

Therefore, when the present invention is applied to an evaporator of a fuel cell device, methanol as raw fuel and water for steam reforming are evaporated and vaporized in an evaporating section and then passed through a lower header tank to a superheat section. Unheated raw fuel entering the lower header tank through the evaporation section
It is led to the superheat section at the flow rate of the mixed gas of methanol and water vaporized, or is evaporated by receiving heat transfer from the upper heat exchange section, enters the superheat section, and is completely evaporated and vaporized from the outlet. A mixed gas of water and water comes out and is supplied to the reformer.

That is, in the fuel cell device, the conventional problem that unvaporized raw fuel does not accompany the vaporized gas from the evaporator to the fuel reformer, and the temperature of the catalyst layer decreases due to the heat of vaporization of the raw fuel. And the effect that the reforming reaction is effectively and stably performed in all the catalyst layers is obtained.

[Brief description of the drawings]

FIG. 1 is an explanatory diagram showing a configuration example of a plate-fin heat exchanger according to the present invention, where A is a top explanatory diagram and B is a front explanatory diagram.

2A is an explanatory side view of the rate fin type heat exchanger of FIG. 1, and FIG. 2B is an explanatory sectional view taken along line CC of FIG. 1B.

FIG. 3 is an overall explanatory view of a distribution passage 7 according to the present invention.

FIG. 4A is an explanatory view of a main part of a distribution passage 7 according to the present invention, and B and C are cross-sectional explanatory views.

[Explanation of symbols]

 1 Heat exchange section 1a Evaporation section 1b Superheat section 2 Inlet header tank 3 Outlet header tank 4 Upper header tank 4a Introducing section 4b Outlet section 5 Lower header tank 6 Partition wall 7 Distribution passage 8,9 Small holes for distribution

 ──────────────────────────────────────────────────続 き Continued on the front page (72) Inventor Katsuo Iwata 1-10 Fuso-cho, Amagasaki-shi, Hyogo Sumitomo Precision Industries, Ltd. F term (reference) 3L065 DA13 3L103 AA05 AA37 BB26 CC12 CC27 DD15 DD17 DD53 DD55 5H027 AA02 BA01

Claims (4)

[Claims] 1. A heat exchanger in which a low-temperature fluid passage is arranged in a direction orthogonal to a downflow direction of a high-temperature fluid passage to form a heat exchange portion, and an upper and lower header tank for a low-temperature fluid is arranged in the downflow direction of the high-temperature fluid passage. In the exchanger, a small hole for distribution is provided in the partition that divides the fluid inlet of the upper header tank into two chambers of primary distribution and secondary distribution, and the distribution amount of the low-temperature fluid from the inlet to each low-temperature fluid passage, A plate fin type heat exchanger that increases near the inlet of the high-temperature fluid passage. 2. The small holes for distribution are arranged by changing the hole diameter, the number of holes, and the injection direction according to the heat load on the high-temperature fluid passage side.
2. The plate fin type heat exchanger according to 1. 3. The plate-fin type heat exchanger according to claim 2, wherein the primary distribution passage of the header tank is a pipe, and the small distribution holes have a jetting direction in a flowing direction of the low-temperature fluid. 4. The heat exchanger is divided by a partition wall that arranges the upper header tank and the low-temperature fluid passage in the flow direction of the low-temperature fluid, and the low-temperature fluid introduced from the upper header tank (inlet) is supplied to the lower header tank. 2. The plate fin type heat exchanger according to claim 1, wherein the plate fin type heat exchanger is configured to be able to pass through the upper header tank (outlet) after passing therethrough and exchanging heat with the high-temperature fluid again.