JPH0534082A - Condensing evaporator - Google Patents

Abstract

(57) [Summary] [Objective] To provide a condensing evaporator which can make a liquid depth shallow while securing a sufficient heat transfer area and can be manufactured by using the conventional manufacturing technique as it is. [Structure] In an oxygen chamber for evaporating liquefied oxygen, an evaporation channel is formed in a vertical direction with an open top and a bottom. The nitrogen chamber 30 for condensing the nitrogen gas is divided into two condensing passages 32, 33, and inlet headers 32a, 33a for introducing the nitrogen gas to both sides of the condensing passages 32, 33 and liquefied nitrogen are derived. Outlet headers 32b and 33b are provided. Condensation channels 32 and 33 of the nitrogen chamber 30 are 4 in the direction of fluid flow.
It forms a downward slope of 5 degrees or less.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a condensing evaporator, and more specifically, a plate fin type heat exchanger in which a plurality of evaporating chambers and condensing chambers are alternately formed by a large number of vertical partition plates in a liquid medium. A condensing evaporator which is immersed and heat-exchanges the liquid medium in the evaporation chamber and the gas fluid in the condensation chamber to evaporate and vaporize the liquid medium and to condense and liquefy the gas fluid, especially for use in an air liquefaction separation device. It relates to a suitable large-scale condenser evaporator.

[0002]

2. Description of the Related Art A condenser evaporator used in a double rectification column of an air liquefaction separation apparatus is partitioned by a plurality of parallel partition plates in the vertical direction, and an oxygen chamber which is an evaporation chamber and a nitrogen which is a condensation chamber. A so-called plate fin type heat exchanger in which two chambers are alternately stacked adjacent to each other is often used.

11 to 14 show a conventional condensation evaporator using this type of plate fin type heat exchanger. FIG. 11 is an oxygen chamber (evaporation chamber), and FIG. 12 is a nitrogen chamber (condensation chamber). ), And FIG. 13 shows a perspective view of the plate fin type heat exchanger. In each of the following figures, the solid line arrow indicates the liquid flow direction, and the chain line arrow indicates the gas flow direction.

First, as shown in FIG. 11, the oxygen chamber 2 of the plate fin type heat exchanger 1 is provided with a heat transfer plate therein to form a large number of vertical evaporation passages 3 and 3. The upper and lower ends of the evaporation channel 3 are opened so that the lower end serves as an inlet 4 for liquefied oxygen LO and the upper end serves as an outlet 5 for a mixed flow of oxygen gas GO and liquefied oxygen LO. This oxygen chamber 2
Liquefied oxygen LO accumulated in the bottom space of the upper tower 6 by the heat exchanger 1
It is filled with liquefied oxygen LO by being immersed therein, and the liquefied oxygen LO in the oxygen chamber 2 exchanges heat with the nitrogen gas GN in the adjacent nitrogen chamber 7, and a part thereof is evaporated to generate oxygen gas. It becomes a bubble of GO and goes up the evaporation flow path 3. The liquefied oxygen LO forms a circulation flow inside and outside the heat exchanger 1 due to the rising force of the oxygen gas GO and the density difference due to gas-liquid mixing. Further, a part of the liquefied oxygen LO and the oxygen gas GO is led out as a product or the like.

On the other hand, as shown in FIG. 12, the nitrogen chamber 7 is
Condensation channel 8 in the up-and-down direction in a room where each end of the four circumferences is sealed,
A large number of headers 8 are formed, and the upper and lower ends of the condensing channel 8 are provided above and below one end of the nitrogen chamber 7, respectively.
And the lower tower 13 through the pipes 11 and 12. In the nitrogen chamber 7, the nitrogen gas GN in the upper part of the lower tower 13 is introduced through the pipe 11 and the header 9 in the upper part to the gas introduction part 15.
It is introduced into the condensing channel 8 as a downward flow via a, and the condensing channel 8
The liquefied nitrogen LN condensed in (1) is led out from the lower header 10 and the pipe 12 via the condensate outlet 15b. In addition, the non-condensed gas GX in the nitrogen gas GN is
It is led out from the purge nozzle 10a provided in the upper part of 0.

The oxygen chamber 2 and the nitrogen chamber 7 as described above are shown in FIG.
As shown in FIG. 3, a plurality of parallel partition plates (plates) 14 are arranged in the vertical direction and stacked. Further, corrugation fins that are bent and formed in a corrugated shape are used for the heat transfer plates that form the channels 3 and 8.

As described above, in the conventional condenser evaporator, both flow paths of the oxygen chamber 2 and the nitrogen chamber 7 of the heat exchanger 1 are arranged in the vertical direction, and heat is exchanged between oxygen and nitrogen in a countercurrent state. The ones were common.

[0008]

As shown in FIG. 14, in a condensing evaporator incorporated in a rectification tower of a large-scale air liquefaction separation apparatus which requires a large number of plate fin type heat exchangers 1 as described above, as shown in FIG. In the bottom space of the upper tower 6 of the rectification tower,
A large number of heat exchangers 1 are arranged radially around the inner cylinder 15 or irregularly to increase the heat transfer area of the condensation evaporator, but the diameter of the outer cylinder of the condensation evaporator is large. In addition, there is a drawback that the manufacturing cost increases.

Further, in the above condensation evaporator, since the entire heat exchanger 1 is used by being immersed in liquefied oxygen LO,
The condensation evaporator could not function unless a large amount of liquefied oxygen LO was stored in the space. For this reason, it takes a long time to start up the apparatus, and the amount of oxygen released at the time of stoppage is large, resulting in loss of power costs and the like. In addition, it is not preferable in terms of security measures to be prepared in case of emergency.

Further, depending on the liquid depth of the liquefied oxygen LO, the upper tower 6
Since the boiling point of the liquefied oxygen LO in the lower part of the bottom space of the liquefied oxygen increases, the liquefied oxygen LO flowing from the lower part of the oxygen chamber 2 into the evaporation flow path 3 is supercooled. Therefore, in the lower part of the oxygen chamber 2, the liquefied oxygen LO rising in the evaporation passage 3 must be heated to the boiling start temperature by convective heat transfer with low heat transfer efficiency, which lowers the heat transfer efficiency of the flow path 3. Was there.

When the liquid depth of the liquefied oxygen is large, the boiling point of the liquefied oxygen rises, the temperature difference between the liquefied oxygen and the nitrogen side becomes small, and the amount of heat exchanged in the set heat transfer area decreases. Therefore, in order to keep the amount of heat of exchange constant, it is necessary to keep the temperature difference constant, but this operating method is usually performed by raising the operating pressure of the lower column 13 in proportion to the rise in the boiling point of liquefied oxygen. . Therefore, the pressure of the raw material air, which is the inlet fluid of the lower tower 13, is increased. This increase in the raw material air pressure increases the power of the air compressor, resulting in an increase in power cost.

In order to reduce the influence of the liquid depth of the liquefied oxygen, Japanese Patent Application Laid-Open No. 60-17601 has proposed a liquid-medium-flow-type condensation evaporator which evaporates the liquefied oxygen in the oxygen chamber while flowing it down. However, it requires additional equipment such as a liquefied oxygen pump to circulate the liquefied oxygen after it flows down to the upper part of the condensation evaporator. Further, Japanese Patent Application Laid-Open No. 62-213698 proposes means for changing the characteristics of the heat transfer surface in the vertical direction, controlling the liquid pressure of liquefied oxygen, and the like.
Conventionally, it has been desired to improve the heat exchange efficiency of this type of condensation evaporator.

Further, in the nitrogen chamber 7 on the condensation side, the condensation flow path 8 is formed in the vertical direction, and the nitrogen gas GN flows down while condensing, so that the amount of liquefied nitrogen increases in the lower part of the flow path 8. Since it becomes a thick liquid film and covers the surface of the heat transfer surface, this becomes a heat resistance layer and deteriorates the heat transfer performance.

In order to reduce the influence of the liquid depth of the liquefied oxygen, the flow paths 3 and 8 may be shortened to lower the height of the heat exchanger 1. However, in order to shorten both flow passages 3 and 8 while ensuring the heat transfer area of the heat exchanger 1, either the width direction of both flow passages should be increased or the thickness (lamination) direction should be increased. Absent. If the thickness direction is increased, the number of stacked stages of the heat exchanger 1 is increased, the number of constituent parts of the heat exchanger 1 is increased, and this is a factor of increasing the cutting cost and the manufacturing cost for stacking.

When the width direction is increased, the condensation flow path 8
If the height of the distributor section (gas introduction section 15a and condensate derivation section 15b) in the direction of the condensation channel 8 is not increased, the nitrogen gas is evenly distributed to each condensation channel,
Since the condensate cannot be merged, the height of the heat exchanger 1 cannot be lowered in spite of shortening both flow paths in order to reduce the liquid depth of liquefied oxygen.

Further, in the heat exchanger having the conventional structure, the mounting positions of the headers 9 and 10 are limited to both ends due to its structure. Therefore, when the width direction and the thickness direction are increased, the above-mentioned per core of the heat exchanger is used. The distributor part, header, piping, etc. must be enlarged, which causes the height of the heat exchanger to increase.

That is, in order to manufacture a large-scale condensing evaporator having a large throughput in a compact size and at a low cost, a heat exchanger having a conventional structure cannot cope with the problem. On the other hand, if the heat exchanger type is changed to a flow-down type or the like, the conventional manufacturing technology cannot be utilized, and the cost of designing and manufacturing will increase significantly.

[0018] Therefore, an object of the present invention is to provide a condensing evaporator which can make a liquid depth shallow while securing a sufficient effective heat transfer area and can be manufactured by using the conventional manufacturing technique as it is.

[0019]

In order to achieve the above-mentioned object, the condensation evaporator of the present invention is a plate fin type heat exchanger in which a large number of evaporation chambers and condensation chambers are alternately laminated with partition plates. In the condensing evaporator used by being immersed in the liquid medium in the container, the heat exchanger forms an evaporation channel of the evaporation chamber for evaporating the liquid medium in a vertical direction with the upper and lower sides opened, and condenses the gas fluid. It is characterized in that a gas inlet and a condensate outlet are provided on both sides of the condensing chamber, and the condensing channel of the condensing chamber is formed in a downward gradient of 45 degrees or less toward the horizontal or fluid flow direction.

Further, in the condensing evaporator of the present invention, the heat exchanger is arranged in the container such that the condensing flow path is horizontal or has a downward gradient of 45 degrees or less in a fluid flow direction. That the flow path length of the evaporation flow path of the heat exchanger is a flow path length that does not substantially cause a supercooling region of the evaporation liquid medium, and the condensation flow path of the condensation chamber is perforated. The condensing chamber has a condensing part for condensing a gas fluid in the upper part and a liquid passing part for flowing a condensate in the lower part, and the condensing chamber is formed in a fluid flow direction. A plurality of parts are formed separately, and a gas introduction part and a condensate discharge part are provided on both sides of each of the divided condensing chambers, and the heat exchanger has a height dimension that is in the fluid flow direction of the condensing chamber. Size and / or smaller than the stacking direction size of both chambers, before A container is divided into a plurality of upper and lower stages, at least one heat exchanger is arranged in each stage, and a liquid descending port for letting a liquid medium flow down to a lower stage and a gas ascending port for raising liquid medium vapor evaporated in an evaporation chamber And at least one set of a gas supply pipe for supplying a gas fluid to the gas introduction part of the condensation chamber of each heat exchanger and a liquid discharge pipe for discharging the condensed liquid from the condensed liquid discharge part, and in the container In which a condensate storage chamber is provided.

[0021]

[Operation] According to the above configuration, it is possible to substantially eliminate the supercooling zone in the evaporation passage due to the large liquid depth of the liquid medium, and prevent the heat transfer performance from being deteriorated by the liquid film in the condensation passage. be able to. In addition, since the condensing channel is formed in a horizontal or downward slope of 45 degrees or less, a plurality of condensing chambers are provided in the same heat exchanger, and the header is mounted in the direction in which the evaporation channel is opened, There is no need to increase the height of the distributor, and the heat exchanger 1
The height of the heat exchanger can be reduced while securing the length of the heat transfer surface on the condensation side required for each base.

[0022]

[Examples] In the following, the evaporation chamber of the heat exchanger is an oxygen chamber, the condensation chamber is a nitrogen chamber, the liquid medium to be evaporated is oxygen, the gas fluid to be condensed is nitrogen, and the container is the upper column lower space of the double rectification column. That is, it will be described in more detail based on the drawings in which the present invention is applied to the main condenser evaporator of the air liquefaction separation device.
The same elements as those in the conventional example are designated by the same reference numerals and detailed description thereof will be omitted.

First, FIGS. 1 to 3 show a first embodiment of a condensation evaporator according to the present invention. FIG. 1 is a sectional view showing a nitrogen chamber portion of a heat exchanger, and FIG. 2 is a sectional view showing an oxygen chamber portion thereof. It is a figure and Drawing 3 is a perspective view of a heat exchanger.

The condensing evaporator has a heat exchanger 22 in a space (container) 21 formed between the upper tower 6 and the lower tower 13 of the double rectification tower. Oxygen chamber 23
Is a bending line of a heat transfer member such as a corrugation fin, preferably a perforate fin having a fin pitch of 3 mm or less (see FIG. 4) in each chamber partitioned by a vertical partition plate 24 in a similar manner to the conventional one. Has a large number of evaporation flow paths 25 arranged in the vertical direction.

The perforate fin Fp shown in FIG. 4 is used for the evaporation passage 25 in order to prevent the concentration of hydrocarbons, especially acetylene, contained in the liquefied oxygen in the oxygen chamber 23. That is, a large number of holes h provided in the fin Fp
Since the liquefied oxygen can freely flow in and out between the fins via the, the concentration of hydrocarbons in the liquefied oxygen for each fin can be made uniform, and the concentration of hydrocarbons can be prevented. It is also conceivable to use the serrate fins Fs shown in FIG. 5 as fins capable of preventing the concentration of hydrocarbons in the main evaporation passage 25. However, when the serrate fins Fs are used in the evaporation flow path 25, compared with the perforate fins Fp, the pressure loss increases even under the same flow rate, and the circulation flow rate of liquefied oxygen decreases and the evaporation heat transfer decreases.

In the oxygen chamber 23 thus formed, a circulation flow inside and outside the heat exchanger similar to that shown in FIG. 11 is formed, and the liquefied oxygen exchanges heat with the nitrogen gas in the adjacent nitrogen chamber 30, Part of the gas evaporates to form bubbles of oxygen gas, which rises in the evaporation flow path 25.

On the other hand, the nitrogen chamber 30 is provided with a vertical partition plate 2.
Sidebars 31, 31 on the four sides of each room divided by 4
Is provided to block the oxygen side from the nitrogen chamber, a part of the side bar 31 is opened, and inlet headers 32a and 33a for introducing nitrogen gas into the upper side opening are provided in the lower side opening. Outlet headers 32b and 33b for discharging condensed liquefied nitrogen are provided, respectively.

The nitrogen chamber 30 includes an inlet header 32a provided at an upper portion on one side to an outlet header 32b provided at a lower central portion and an inlet header 33a provided at an upper central portion to an outlet provided at a lower portion on the other side. It is partitioned by the partition bar 34 up to the header 33b, and the distributor 3 of the inlet header part in both partitions (core)
Condensation channels 32 and 33 are provided between 2c and 33c and the distributors 32d and 33d of the outlet header portion, respectively.

The condensing flow paths 32, 33 have a bent line of perforate fins or serrate fins having a fin pitch of 3 mm or less and a downward gradient of 0 to 45 degrees from the inlet side to the outlet side in the fluid flow direction. It is formed by arranging so that. In addition, both condensing channels 32, 33
At the bottom, the condensate passages 32e, 3e formed by corrugation fins or the like having a large fin pitch for flowing the liquefied nitrogen condensed in the condensing passages 32, 33 to the outlet side.
3e is provided.

The use of perforate fins or serrate fins in the condensing channels 32 and 33 allows the liquid produced by condensation to flow downward due to gravity, and has a higher condensation heat transfer than other fin shapes. This is because the pressure loss on the condensation side is small compared to the dense heat transfer fins.

The evaporation passage 25 and the condensation passages 32, 33
Is formed by fins having a pitch of 3 mm or less based on the knowledge and results obtained from the viewpoints of evaporation, condensation heat transfer improvement, heat transfer density improvement, pressure loss, and the like.

The nitrogen gas in the upper part of the lower tower 13 is branched from the pipe 11 to the inlet headers 32a and 33a, and then, from the distributors 32c and 33c to the condensation passages 32 and 3, respectively.
Introduced into 3 to perform heat exchange with the oxygen gas in the adjacent oxygen chamber 23 and condense into liquefied nitrogen. The liquefied nitrogen flows through the condensing channels 32 and 33 and the condensate channels 32e and 33e, collects from the distributors 32d and 33d on the outlet side to the outlet headers 32b and 33b, and is led out through the pipe 12.

As described above, the condensing channels 32 and 33 are formed in the lateral channel having a downward slope, and the gas introducing section and the condensate derivation section are provided on both sides of the condensing channels 32 and 33. Even if the height of the heat exchanger 22 is lowered to reduce the liquid depth, the dimension of the condensation transmission surface in the flow direction of the condensed fluid is lengthened by a necessary amount to secure a sufficient condensation transmission surface. Is possible. However, this flow path length does not need to be set many times longer than the evaporation flow path length because the boiling condensation heat transfer coefficient is generally one digit or more larger than in the case of boiling liquid / gas. If the descending slope angle is 45 degrees or more, the effect of lowering the height of the heat exchanger is impaired.

Further, by dividing the flow path on the condensation side into a plurality of parts in the same heat exchanger, and by using serrate fins, perforate fins, etc. in the flow path, it is also divided in the same heat exchanger. Each condensing flow path 32, 33
By providing the condensate flow paths 32e and 33e in the lower part of the flow path so that the condensate is guided to the outlet side, it is possible to reduce the thickness of the liquid film condensed on the surface of the condensation heat transfer surface in the upper part of each flow path. ,
The effect of the heat transfer resistance layer due to the liquid film can be further reduced, and the effective heat transfer area on the condensation side can be increased.

Generally, the heat transfer coefficient of such a heat exchanger is smaller on the condensing side than on the evaporating side. Therefore, if the condensing side effective heat transfer surface is increased, the heat exchanger can be downsized.
In the present invention, the condensate flow path is lateral and the condensate is removed from the transmission surface by gravity to increase the effective transmission surface.

Therefore, it is possible to increase the effective heat transfer area of the nitrogen chamber 30 on the condensing side and shorten the length of the evaporation passage 25 of the oxygen chamber 23 on the evaporating side, as compared with the heat exchanger of the conventional structure. It is possible to reduce the height and downsize. Further, since the height of the heat exchanger is lowered, the influence of the liquid depth of liquefied oxygen, that is, the convection heat transfer area due to supercooling can be reduced, and the evaporation efficiency on the evaporation side can be improved.

Therefore, the height dimension of the heat exchanger 22 is made smaller than the dimension in the fluid flow direction of the condensing channels 32, 33 and the dimension in the stacking direction of the two chambers 23, 30 so that the height of the heat exchanger 22 is smaller than that of the conventional one. It is possible to achieve the same or better performance with a small heat exchanger. Moreover, since the liquid depth can be made shallow by reducing the height of the heat exchanger, it is possible to make the upper tower lower space 21 that serves as the container of the condensation evaporator small, and it is possible to significantly reduce the manufacturing cost. Furthermore, since the amount of liquefied oxygen required for the condenser evaporator to function can be reduced, the start-up time of the air liquefaction / separation device can be shortened, and the amount of oxygen released during shutdown can also be reduced, reducing the power consumption of the air compressor. Can be realized and security equipment can be reduced.

In addition, since the heat exchanger 22 having the above structure is used by immersing it in liquefied oxygen as in the case of the heat exchanger having the conventional structure, the amount of flow down is smaller than that of the flow down type in which liquefied oxygen is flowed down. It is not necessary to provide a control mechanism or a pumping means for circulating liquefied oxygen after flowing down in the upper part, and the manufacturing process is also the same as the conventional one, in which partition plates and heat transfer plates are alternately laminated in a predetermined direction. After that, it can be performed by a method of integrally joining, for example, by brazing. Therefore, it is possible to use the conventional manufacturing technology and device configuration of the condenser evaporator using the plate fin type heat exchanger, so the heat exchange performance confirmation experiment and liquid circulation confirmation experiment by adopting a new structure. It is possible to manufacture and use immediately without performing a manufacturing test.

The heat exchanger 22 having the above structure is shown in FIGS.
As shown in, it can be placed in the upper tower lower space 21 which is a container. The upper tower lower space 21 is provided with horizontal partition plates 40, which are two upper and lower liquid storage portions 41a and 41b.
It is divided into A nitrogen gas rising pipe 42 is provided in the center of the partition plate 40, and the nitrogen gas rising pipe 42 is provided with a pipe 11 for distributing the nitrogen gas to the inlet headers 32 a and 33 a of each heat exchanger 22. ing. Further, the partition plate 40 has a liquid descending port 43 on the outer periphery of the nitrogen gas rising pipe 42.
And a liquid lowering port / gas rising port 44 between the heat exchangers 22 are provided. Further, a condensate storage chamber 45 for storing the liquefied nitrogen condensed in the heat exchanger 22 is provided at the bottom of each liquid reservoir 41a, 41b.

Liquid collecting section 41a from the rectification stage to the upper stage of the upper tower 6
The liquefied oxygen that has flowed down to the inside of the heat exchanger 22 circulates inside and outside the oxygen chamber, and a part of it evaporates into oxygen gas, which rises to the upper column rectification stage. Further, a part of the liquefied oxygen overflows from the liquid descending ports 43 and 44, flows down to the lower liquid reservoir 41b, heat-exchanges with the nitrogen gas in the lower heat exchanger 22 and evaporates to become oxygen gas. Ascends through the gas rise port 44.

The nitrogen gas introduced from the lower tower 13 into the nitrogen chamber through the nitrogen gas rising pipe 42, the pipe 11, and the inlet headers 32a and 33a is liquefied by heat exchange with the liquefied oxygen to become liquefied nitrogen, and the outlet It is led out to the condensate storage chamber 45 from the headers 32b and 33b through the pipe 46. The liquefied nitrogen stored in the upper condensate storage chamber 45 flows down into the lower condensate storage chamber 45, merges with the liquefied nitrogen liquefied in the lower heat exchanger 22, and then is led out to the pipe 12. The nitrogen gas rising pipe 42, the pipe 11, the condensate storage chamber 45
Is provided with a nozzle 47 for discharging the non-condensed gas.

By arranging the heat exchangers 22 in the upper and lower stages in this manner, the diameter of the upper tower lower space (container) 21 can be further reduced. Furthermore, the liquid reservoir 41
By providing the condensate storage chamber 45 at the bottoms of a and 41b, the amount of liquefied oxygen stored in the liquid reservoir can be reduced. By reducing the amount of the stored liquid of liquefied oxygen, the start-up time of the air liquefaction separation device can be shortened, and the amount of liquefied oxygen released at the time of stop can be reduced.

Here, in the condensing evaporator having the structure of the above-mentioned embodiment and the condensing evaporator having the above-mentioned conventional structure, the size and the number of heat exchangers necessary for performing the treatment under the same conditions are compared with the container diameter. The results obtained are shown in Table 1.

The treatment conditions were as follows: the oxygen pressure on the evaporation side was 0.6 kg / cm ² G, and the nitrogen pressure on the condensation side was 5.2 kg / cm ^2.
The boiling point of oxygen is −178.9 ° C., and the boiling point of nitrogen is −176.5 ° C.

[0045]

[Table 1]

As can be seen from Table 1 above, the number of heat exchangers can be reduced and the diameter of the container can be reduced, so that the cost and size can be greatly reduced. It should be noted that the size of one block of the heat exchanger is about half the height as compared with the conventional one, and the width and length can be arbitrarily selected, and can be determined in consideration of other conditions. The degree of freedom is great.

In the above specifications, the liquefied oxygen in the lower part of the heat exchanger is heated to -177.5 ° C depending on the liquid depth when the height of the heat exchanger is 1800 mm, but the height is 900.
In the case of mm, the temperature can be reduced up to −178.2 ° C., so the temperature difference from the condensation side is increased by about 30%, and the heat transfer area can be reduced accordingly.

8 to 10 show another embodiment of the present invention. In the figure, only the condensation chamber portion is shown, and the evaporation chamber is not shown.

The condensing chamber 50 shown in FIG. 8 has a condensing channel 51 formed horizontally. In this way, the condensation channel 5
Even if you set 1 horizontally, you can expect some effect,
In order to promote the flow of the condensate, it is preferable that the entire heat exchanger is tilted and installed in the container so that the condensing flow path has a downward gradient. When the heat exchanger is installed in a tilted manner, it is preferable to consider the angle of the evaporation flow passage at the time of manufacture so that the evaporation flow passage is in the vertical direction.

The condensing chamber 52 shown in FIG.
Two 3 are provided at both ends, and the outlet header 54 is provided at one location in the center. In this way, by providing the outlet header or the inlet header at one location in the central portion, the number of pipe connections can be reduced.

The number of divisions of the condensing chamber 55 is appropriately set according to the maximum size of the heat exchanger and the necessary and sufficient condensing flow path length. As shown in FIG. 10, it is divided into three or more sections. You can also do it.

[0052]

As described above, in the condensation evaporator of the present invention, the evaporation passage of the heat exchanger is formed in the vertical direction, and the condensation passage is formed in the lateral direction, so that the condensation passage is required. Since the evaporation flow path was shortened and the height of the heat exchanger was reduced while ensuring a sufficient condensation transfer surface, the efficiency of the condensation evaporator can be greatly improved, and the large-scale condensation evaporator can be made smaller and less costly. Can be achieved. Also, a multi-stage type large-capacity condenser evaporator can be easily manufactured with a sufficiently shallow liquid depth and only by conventional manufacturing techniques.

Further, since the technology of the conventional condenser evaporator can be utilized as it is, it can be carried out immediately. Especially, by using it for the main condenser evaporator of a large-sized air liquefaction separation apparatus, the manufacturing cost of the apparatus can be reduced. Not only that, the operating cost can be reduced.

[Brief description of drawings]

1 is a cross-sectional view showing a first embodiment of a condensing evaporator of the present invention and showing a nitrogen chamber portion of a heat exchanger.

FIG. 2 is a sectional view showing an oxygen chamber portion of the same.

FIG. 3 is a perspective view of the heat exchanger of the same.

FIG. 4 is an enlarged perspective view of a perforate fin.

FIG. 5 is an enlarged perspective view of a serrate fin.

FIG. 6 is a vertical cross-sectional view showing a state of being assembled in a rectification column.

FIG. 7 is a transverse sectional view of the same.

FIG. 8 is a sectional view showing another embodiment of the condensing chamber.

FIG. 9 is a sectional view showing another embodiment of the condensing chamber.

FIG. 10 is a sectional view showing another embodiment of the condensing chamber.

FIG. 11 is a sectional view showing an oxygen chamber portion of a conventional condensing evaporator.

FIG. 12 is a sectional view showing a nitrogen chamber portion of the same.

FIG. 13 is a perspective view of the heat exchanger of the same.

FIG. 14 is a transverse sectional view showing a state of arrangement of heat exchangers.

[Explanation of symbols]

6 ... Upper tower 13 ... Lower tower 21 ... Space 22
… Heat exchanger 23… Oxygen chamber 24… Partition plate 25
... Evaporation channel 30 ... Nitrogen chamber 32, 33 ... Condensing channel 32a, 33a ... Inlet header 32b, 33b
... outlet headers 32e, 33e ... condensate flow path 34 ...
Partition bar 40 ... Partition plates 41a, 41b ... Liquid reservoir 45 ... Condensate storage chamber

Claims (9)

[Claims] 1. A condensing evaporator in which a plate fin type heat exchanger in which a large number of evaporating chambers and condensing chambers are alternately laminated via partition plates is used by being immersed in a liquid medium in a container. Forms an evaporation channel of an evaporation chamber for evaporating a liquid medium in a vertical direction in which the upper and lower sides are opened, and a gas introduction part and a condensed liquid discharge part are provided on both sides of a condensation chamber for condensing a gas fluid, A condensing evaporator, characterized in that the condensing flow path of the chamber is formed in a horizontal direction or a downward gradient of 45 degrees or less toward the fluid flow direction. 2. The heat exchanger is arranged in the container such that the condensing channel is horizontal or has a downward slope of 45 degrees or less toward a fluid flow direction. 1. The condensation evaporator according to 1. 3. The condensation according to claim 1, wherein the length of the evaporation passage of the heat exchanger is such that the supercooled region of the evaporated liquid medium does not substantially occur. Evaporator. 4. The condensing evaporator according to claim 1, wherein the condensing channel of the condensing chamber is formed of a perforate fin or a serrate fin. 5. The condensing evaporator according to claim 1, wherein the condensing chamber has a condensing part for condensing a gas fluid in an upper part and a liquid passing part for flowing a condensate in a lower part. . 6. The condensing chamber is divided into a plurality of parts in the fluid flow direction, and a gas inlet and a condensate outlet are provided on both sides of each of the divided condensing chambers. 1. The condensation evaporator according to 1. 7. The condenser-evaporator according to claim 1, wherein the heat exchanger has a height dimension smaller than a fluid flow dimension of the condensing chamber and / or a laminating dimension of both chambers. 8. The container is divided into a plurality of upper and lower stages, at least one heat exchanger is arranged in each stage, a liquid descending port for allowing a liquid medium to flow down, and a liquid medium vapor evaporated in an evaporation chamber. At least one of a gas rising port for raising the temperature, a gas supply pipe for supplying a gas fluid to the gas introducing portion of the condensing chamber of each heat exchanger, and a liquid outlet pipe for leading the condensed liquid from the condensed liquid outlet.
The condenser evaporator according to claim 1, wherein the condenser evaporator is provided as a set. 9. The condensation evaporator according to claim 1, wherein a condensate storage chamber is provided in the container.