JPH0783801B2 - Evaporator and cryogenic separator for carbon monoxide equipped with evaporator - Google Patents

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an evaporator having a rectification function and a carbon monoxide deep-cooling separator exclusively utilizing the properties of the evaporator.

[0002]

2. Description of the Related Art Conventionally, as an evaporator having a rectification function, for example, one shown in Japanese Patent Publication No. 47-23161 is known. This device is a plate fin type heat exchanger in which elements for high temperature fluid and elements for low temperature fluid are alternately and adjacently arranged so that heat is exchanged between them. The target liquid is vaporized and taken out as gas, while the high temperature fluid element performs rectification by bringing the decompressed liquid component and the inflowing gas into gas-liquid contact, and the high boiling point substance from the bottom of this high temperature fluid element. It is designed to take out a rich condensate.

[0003]

Since the above device is composed of a plate fin heat exchanger having excellent heat transfer performance, heat exchange between the high temperature fluid element and the low temperature fluid element is active due to its structure. The temperature distribution of the fluid on the low temperature side (evaporation side) and the high temperature side (condensation side) in the device is shown in FIG.
As shown by the curves C1 and C2 of 1. That is,
Assuming that the height necessary for sufficiently performing the rectification in the high temperature fluid side element is Hd, the heat exchange in this device is too active, and thus the height is lower than the required rectification height Hd. At Hh, a predetermined amount of gas is all condensed to reach the minimum temperature difference ΔTmin, which makes it difficult to contact gas-liquid at a position higher than this. That is, this apparatus cannot fully utilize the required rectification height Hh, so that even if the height of the entire evaporation apparatus is sufficiently large, the expected rectification effect cannot be obtained.

To avoid such an inconvenience, the thickness of the plate fins is increased or the number of the plate fins is reduced to suppress the amount of heat transfer between the two fluid elements, and the temperature distribution of the high temperature side fluid is shown by the broken line C3 in the figure. However, such suppression of the amount of heat transfer is limited due to the structure and specifications of the heat exchanger, and it is difficult to obtain a remarkable effect. Further, the evaporation performance of the low temperature side fluid may be impaired by suppressing the amount of heat transfer.

In view of the above-mentioned circumstances, the present invention provides an evaporation device capable of sufficiently rectifying a mixed gas by making good use of the latent heat of evaporation of the low-temperature liquid while satisfactorily evaporating the low-temperature liquid. It is an object of the present invention to provide a deep-separation device for carbon monoxide, which makes full use of the properties of the device.

[0006]

According to the present invention, a plurality of evaporation passages extending vertically and having a liquid inlet at a lower portion and an evaporative gas outlet at an upper portion are connected to a lower portion of each evaporation passage. Has a dummy part, a mixed gas inlet in the lower part, and a rectification gas outlet in the upper part, and extends vertically from the height position of the lower end of the dummy part to the height position of the upper end of the evaporation passage. A plurality of rectification passages, and the evaporation passages and the dummy portion and the rectification passages are alternately arranged in a state where they are adjacent to each other in the horizontal direction, and are coupled to each other. In the above, heat exchange is performed between the fluid flowing in the evaporation passage and the portion adjacent to the evaporation passage, and the liquid condensed in the rectification passage due to the heat exchange descends in the portion adjacent to the dummy portion in the rectification passage. Gas and gas-liquid rising up this part while As to touch it is obtained by setting the length of the vaporization channel, the dummy unit, and rectification passages (claim 1).

Further, a sub-evaporation passage is provided above the vaporization passage in a state of being separated from the vaporization passage, and the rectification passage is extended upward to a position adjacent to the sub-evaporation passage so that the rectification passage is It is more effective if the structure is such that heat exchange is performed between the fluid and the fluid in the sub-evaporation passage.

The present invention is also a cryogenic cryogenic separator for carbon monoxide, which exclusively utilizes the properties of the above-mentioned evaporator, and a rectification column for separating carbon monoxide from a mixed gas containing at least carbon monoxide and hydrocarbons. And a reboiler comprising the evaporation device, for evaporating the bottom liquid of the rectification tower, a bottom liquid introduction passage for introducing the bottom liquid of the rectification tower into the evaporation passage from the liquid introduction port, and A gas recirculation passage for deriving the gas in the evaporation passage from the evaporation gas outlet and returning it to the rectification tower.
A mixed gas introduction passage for introducing a mixed gas into the rectification passage from the mixed gas introduction port, and deriving a rectified gas rectified in the mixed gas passage from a rectification gas outlet of the rectification passage, A rectification gas transfer passage introduced as a reflux liquid is provided at the top of the rectification tower (claim 3).

[0009]

In the evaporator according to the first aspect of the present invention, the mixed gas is introduced into the rectification passage from its lower portion, but at the beginning of the introduction, the mixed gas passes through the portion adjacent to the dummy portion, so that heat exchange is performed in this portion. Is not done. Then, when this mixed gas rises to a portion adjacent to the evaporation passage, heat exchange is performed between this mixed gas and the low temperature fluid in the evaporation passage, and while the fluid evaporates, part of the mixed gas condenses. Then, the mixed gas descends to a portion adjacent to the dummy portion, and the mixed gas is rectified by gas-liquid contact between the descending condensate and the ascending mixed gas in this portion. That is, in this device, direct heat exchange is not performed in the lower part of the rectification passage, and direct heat exchange is performed only in the upper portion, so that the mixed gas in the rectification passage is It can be condensed exclusively in the upper part, avoiding condensation in the lower part. Therefore, the entire height region of this rectification passage can be effectively utilized for rectification by gas-liquid contact without wasting the upper part of the rectification passage.

Further, according to the apparatus of claim 2, a liquid having a temperature lower than that of the liquid introduced into the evaporation passage is introduced into the sub-rectification passage to exchange heat with the gas in the rectification passage. By doing so, it is possible to further condense the gas in the rectification passage, that is, the gas that has already reached the minimum temperature difference by heat exchange with the fluid in the evaporation passage, and is discharged from the rectification gas outlet. The purity of the rectification gas can be further increased.

According to the carbon monoxide cryogenic separation device of claim 3, the mixed gas is supplied through the mixed gas introduction passage and the mixed gas introduction port into the rectification passage of the evaporator which is a reboiler, and the rectification is performed. By causing heat exchange between the mixed gas rising in the passage and the bottom liquid in the bottom liquid evaporation passage,
The rectification of the mixed gas can be performed together with the evaporation of the bottom liquid. Then, the rectified gas in the upper part of the rectification passage is introduced into the top of the rectification tower as a high-purity reflux liquid through the rectification gas transfer passage, whereby the high-purity carbon monoxide gas is introduced in the rectification tower. Can be purified.

[0012]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A first embodiment of the present invention will be described with reference to FIGS.

FIG. 7 shows the overall structure of a deep-chill separation system using the evaporation device of the present invention. This system uses a reformed gas such as propane or butane as a raw material and separates carbon monoxide gas from this gas. Here, the evaporator of the present invention enhances the purity of the product gas as described later. Therefore, it is installed to refine the reflux liquid to the top of the rectification column while acting as a reboiler. However,
The apparatus according to claim 3 of the present application is widely applicable to the case of separating carbon monoxide from a mixed gas containing at least carbon monoxide and hydrocarbons.

This system comprises a refrigerator 10, a gas-liquid separator 11, an MS (molecular sieve) adsorption device 12, and a cold insulation box 14. In the cool box 14, a main heat exchanger 16, a rectification column 18, a reboiler 20, a condenser 2
2, 28, the first gas-liquid separator 24, the second gas-liquid separator 25,
Third gas-liquid separator 26, heat exchanger 27, nitrogen gas-liquid separator 3
0, etc., and the evaporator of the present invention is used for the reboiler 20.

The MS adsorption device 12 comprises a main heat exchanger 16
It is connected to the bottom of the reboiler 20 via a mixed gas introduction pipe 32 passing through. The bottom of the reboiler 20 is connected to the middle abdomen of the first gas-liquid separator 24 via a transfer pipe 34, and in the middle of the transfer pipe 34, the heat exchanger 27,
A condenser 28 and an expansion valve 36 are provided. The bottom part of the first gas-liquid separator 24 is connected to the middle part of the rectification column 18 via a condenser 22.

The top part of the reboiler 20 is connected to the middle abdomen of the second gas-liquid separator 25 via the rectification gas transfer pipes 38, 40, and the above-mentioned middle part of the rectification gas transfer pipes 38, 40. The capacitors 22 and 28 are connected. The bottom portion of the second gas-liquid separator 25 is the rectification gas transfer pipe 4
2 is connected to the middle abdomen of the third gas-liquid separator 26, and the bottom of the third gas-liquid separator 26 is connected to the top of the rectification column 18 via a rectification gas transfer pipe 46, An expansion valve 44 is provided in the middle of the rectification gas transfer pipe 42. The reboiler 20 is connected to the bottom of the rectification column 18 via a column bottom liquid introduction pipe 48 and a gas reflux pipe 49.

Next, the structure of the reboiler 20 will be described with reference to FIGS.

As shown in FIG. 2, the reboiler 20 has a heat exchange section 50. A column bottom liquid inlet port 51 is attached to the middle portion of the side surface of the heat exchange section 50, and similarly, a reflux gas outlet port 52 is provided at the upper side surface of the heat exchange section 50.
However, a mixed gas inlet port 53 is mounted on the lower end surface, and a rectification gas outlet port 54 is mounted on the upper end surface. Then, the tower bottom liquid outlet port 4 is connected to the tower bottom liquid inlet port 51.
8 is connected, and similarly, the reflux gas outlet port 52
The gas recirculation pipe 49 is connected to the rectification gas outlet port 54, and the rectification gas transfer pipe 38 is connected to the rectification gas outlet port 54. A gas-liquid separation pipe 56 having a bottom is connected to the mixed gas inlet port 53,
The transfer pipe 34 is connected to the bottom of the gas-liquid separation pipe 56, and the mixed gas introduction pipe 32 is connected to a position above the transfer pipe 34.

As shown in FIGS. 1 and 3 to 6, the heat exchange section 50 is provided with a large number of partition plates 58 made of aluminum or the like and arranged in parallel with each other. Between the columns 58, column bottom liquid evaporation passages 59a and rectification passages 59b are formed alternately.

As shown in FIG. 4 (a), the column bottom liquid evaporation passage 59a is disposed only in the height region H2 of the upper half of the heat exchange section 50, and the portion immediately below it (the heat exchange section 50). A dummy portion 68 is provided in the height region H1 of the lower half portion).

A pair of L-shaped side bars 60a are arranged around the stage forming the column bottom liquid evaporation passage 59a,
As shown in FIG. 5, these side bars 60a are arranged between both partition plates 58 so as to be in close contact with them. These sidebars 60a block part of the upper and lower ends and side ends of the bottom liquid evaporating passage 59a, and a bottom liquid introducing port 62a is formed in the lower part of one side end, and the other side end is formed. An evaporative gas outlet 63a is formed in the upper part. The tower bottom liquid inlet port 51 is installed at a position that closes the tower bottom liquid introduction port 62a, and the reflux gas outlet port 52 is provided at a position that closes the evaporative gas outlet port 63a.
Is installed.

Further, a corrugated plate-shaped fin 64a extending in the vertical direction is provided in the middle part of the tower bottom liquid evaporation passage 59a. A fin 65 is provided below the fin 64a and extends obliquely upward from the tower bottom liquid inlet 62a to the fin 64a, and above the fin 64a is obliquely upward from the fin 64a to the evaporative gas outlet 63a. An extending fin 66 is provided. These fins 6
4a, 65, 66 are made of aluminum or the like, and are joined to the surface of the partition plate 58 by brazing or the like as shown in FIG.

The dummy part 68 is not provided for introducing a fluid into the inside thereof, but is installed below the column bottom liquid evaporation passage 59a for the purpose of merely reinforcing the column bottom liquid evaporation passage 59a. Similar to the side bar 60a
Is surrounded by a fin 7 similar to the above-mentioned fin 64a.
0 is provided exclusively for reinforcement. Also, this dummy part 6
A communication port 71 for degassing is provided at an appropriate position below the position 8.

On the other hand, the rectification passage 59b is shown in FIG.
As shown in (a) and (b), the heat exchanging portion 50 is arranged in the entire area in the vertical direction, that is, in the entire height region including both the height regions H1 and H2. That is, the rectification passage 59b extends vertically from the lower end of the dummy portion 68 to the upper end of the column bottom liquid evaporation passage 59a, and is horizontally adjacent to both the column bottom liquid evaporation passage 59a and the dummy portion 68. It is in the state of doing.

At the side end of the step forming the rectification passage 59b, a side bar 60b is provided to close the side end over the entire area in the vertical direction. These sidebars 60b
Similarly, like the side bar 60a, it is arranged between both partition plates 58 so as to be in close contact with them. As a result, a mixed gas inlet 62b and a rectification gas outlet 63b are formed at the lower end and the upper end of this stage, respectively.
The mixed gas inlet port 53 is attached to a position where the mixed gas inlet port 62b is closed, and the rectified gas outlet port 54 is attached to a position where the rectified gas outlet port 63b is closed. Therefore, as shown in FIG. 2, the mixed gas inlet port 53 is provided at a position lower than the column bottom liquid inlet port 51. Further, a corrugated plate-shaped fin 64b extending in the vertical direction is disposed between both side bars 60b, and the fin 64b is also joined to the surface of both joint plates 58 by brazing or the like.

That is, the heat exchange section 50 shown here includes the partition plate 58, the fins 64a, 65, 66, and the partition plate 5.
8, the fins 64b, the partition plate 58, ... Are laminated in this order, and the column bottom liquid evaporation passage 59 is formed.
The layer formed of a and the dummy portion 68 and the layer formed of the evaporation passage 59b alone are alternately arranged in a horizontally adjacent state.

Next, the refrigerating separation operation of carbon monoxide carried out in this apparatus will be explained.

First, the raw material gas (mixed gas) is the refrigerator 10.
The water that has been cooled by the above method and condensed here is separated by the gas-liquid separator 11. The remaining gas is sent to the MS adsorption device 12, where water and carbon dioxide are removed, and then introduced into the cold insulation box 14 through the mixed gas introduction pipe 32.

This gas exchanges heat with the return gas in the main heat exchanger 16, is cooled, and then is introduced into the mixed gas inlet port 53 of the reboiler 20 through the gas-liquid separation pipe 56 shown in FIG. Since only the mixed gas inlet 62b shown in FIGS. 1B and 4B faces the mixed gas inlet port 53, the gas is introduced from the mixed gas inlet 62b into the heat exchange section 50. Of the rectification passage 59b, that is, the passage surrounded by both side bars 60b, flows upward (arrow B). At the beginning of this inflow, the mixed gas is used for the dummy portion 70.
Direct heat exchange with the bottom liquid is not performed because it flows in the area adjacent to the column bottom liquid.

On the other hand, the bottom liquid of the rectification column 18 is introduced into the bottom liquid inlet port 51 of the reboiler 20 through the bottom liquid introducing pipe 48. The bottom liquid inlet port 51 has a bottom liquid inlet 62 shown in FIGS. 1 (b) and 4 (a).
Since only a is exposed, the tower bottom liquid is transferred from the tower bottom liquid inlet 62a to the tower bottom liquid evaporation passage 59a in the heat exchange section 50,
That is, it flows into the passage surrounded by both side bars 60a (arrow A).

As a result of this introduction, in the upper half of the heat exchange section 50 (that is, in the height region H2), as shown in FIG. 6, the column bottom liquid evaporation passage 59a and the rectification passage 5 are adjacent to each other.
The vaporized gas (arrow A) and the mixed gas (arrow B) of the column bottom liquid respectively flow in 9b, and heat exchange is performed between them.
By this heat exchange, the bottom liquid in the bottom liquid evaporation passage 59a is heated and evaporated, and the evaporated gas is returned to the bottom of the rectification column 18 through the reflux gas outlet port 52 and the reflux gas passage 49 (arrow AG). ). At the same time, the mixed gas in the rectification passage 59b cooled by the heat exchange partially condenses and descends, and the descending condensate comes into contact with the rising mixed gas to rectify the mixed gas. A rectification gas having a high carbon monoxide concentration is generated at the top of the rectification passage 59b.

Here, the condensate collects from the mixed gas inlet port 53 at the bottom of the gas-liquid separation pipe 56 and passes from the bottom along the transfer pipe 34 (arrow BL) to the heat exchanger 27,
It is introduced into the capacitor 28. Liquid nitrogen, which is a cold source, is supplied to this condenser 28 from a nitrogen gas-liquid separator 30, and the mixed gas is cooled by heat exchange with this and the first gas-liquid separation through the expansion valve 36. Sent to the container 24. The liquid at the bottom of the first gas-liquid separator 24 is
It is introduced into an appropriate portion of the rectification column 18 through a condenser 22.

On the other hand, the rectified gas that has risen to the top of the reboiler 20 enters the rectified gas transfer pipe 38 from the rectified gas outlet port 54, is cooled by the condensers 22 and 28, and then is subjected to the second gas-liquid separation. It is introduced into the container 25. Then, it is introduced into the third gas-liquid separator 26 from the bottom of the second gas-liquid separator 25 through the rectification gas transfer pipe 42 and the expansion valve 44, and the rectification gas is introduced from the bottom of the second gas-liquid separator 26. It is supplied as a reflux liquid to the top of the rectification column 18 through the transfer pipe 46.

As described above, the high-purity gas purified from the mixed gas in the reboiler 20 is introduced into the top of the rectification column 18 as a reflux liquid, so that the rectification column 18 has extremely high-purity carbon monoxide. The gas is refined, and this gas is taken out to the outside of the cool box 14 as product carbon monoxide gas through the product gas outlet passage 47.

As described above, in this device, the cool box 14
First, the mixed gas introduced into the reboiler 20 is introduced into the bottom of the reboiler 20 and passed through the rectification passage 59b, and heat exchange between this gas and the bottom liquid in the bottom liquid evaporation passage 59a is performed. Thus, it is possible to efficiently evaporate the bottom liquid and rectify the mixed gas in the rectification passage 59b. Moreover,
A dummy part 68 into which no fluid is introduced is arranged below the column bottom liquid evaporation passage 59a, and a region (total height region) adjacent to both the dummy part 68 and the column bottom liquid evaporation passage 59a.
The rectification passage 59b is disposed in the lower part, that is, the heat exchange is not performed directly in the lower portion, that is, in the portion adjacent to the dummy portion 68, and the heat exchange is performed only between the rectification passage 59b and the bottom liquid evaporation passage 59a in the upper portion. Therefore, the temperature distribution of the mixed gas is as shown by the broken line C3 in FIG. 11, and the above mixed gas can be condensed at the upper part. Therefore, the conventional device, that is, both passages 59 in the entire height region
Like the device for exchanging heat between a and 59b, the rectification passage 5
The disadvantage that all a predetermined amount of gas is condensed at the lower part of 9b does not occur, and effective rectification can be performed by utilizing the entire height of the rectification passage 59b.

Particularly, in the system shown in FIG. 7, the evaporator of the present invention is skillfully used as the reboiler 20, and the high-purity rectified gas obtained in the rectification passage 59b is used as the reflux liquid in the rectification column. Since it is supplied to the top of the column 18, by using the double rectification column as in the prior art or without refluxing a part of the product gas, the reboiler 20 also serves as the rectification device. A high-purity reflux liquid can be efficiently generated, whereby a high-purity product CO gas can be obtained at low cost.

Next, a second embodiment will be described with reference to FIGS.

Here, in the layer on the column bottom liquid evaporation passage 59a side, in addition to the column bottom liquid evaporation passage 59a and the dummy portion 68, sub-evaporation is performed in a height region H3 further above the column bottom liquid evaporation passage 59a. A passage 59a 'is provided, and a rectification passage 59b is provided to a position adjacent to the sub-evaporation passage 59a'.
Has been extended upwards. That is, this rectification passage 59
b is installed over the entire height regions H1, H2, H3. The sub-evaporation passage 59a ′ is the bottom liquid evaporation passage 59.
Similarly to a, the side bar 60a 'and the fins 64a', 6
5'and 66 ', a liquid inlet 62a' is provided at the lower end, and an evaporative gas outlet 63a 'is provided at the upper end. Inside the sub-evaporating passage 59a' and the column bottom liquid evaporating passage. 5
The inside of 9a is separated from each other by a horizontal partition plate 72.

According to this structure, a fluid having a temperature lower than that of the fluid in the bottom liquid evaporation passage 59a is provided in the sub-evaporation passage 59a '(for example, liquid nitrogen in the system shown in FIG. 7).
Is introduced from the liquid introduction port 62a ', the rectification gas in the rectification passage 59b can be further cooled and condensed by heat exchange with this fluid. That is, as shown in FIG. 10, the rectified gas that has passed through the height region H2 in the rectification passage 59b and is cooled to the minimum temperature difference ΔTmin with respect to the evaporation side is heated by the low temperature fluid in the height region H3. It can be further cooled and condensed by exchange. As a result, the rectification gas outlet 63 at the upper end of the sub-evaporation passage 59a 'is provided.
It is possible to take out a rectified gas of higher purity from b.

The present invention is not limited to the above embodiments, but the following modes can be adopted as examples.

(1) The distillation apparatus of the present invention is not limited to the reboiler 20 as described above, but can be used as an evaporation apparatus for various liquids. For example, in the system shown in FIG. 7, the nitrogen gas-liquid separator 30 which is an evaporator for liquid nitrogen.
It is also possible to apply the present invention to.

(2) The dummy portion 68 in the present invention is not limited to the structure shown in the above embodiment, and may be a reinforcing member having another structure, for example, a thick plate.

[0043]

As described above, according to the present invention, the following effects can be obtained.

First, in the distillation apparatus according to the first aspect of the present invention, heat exchange between the mixed gas in the rectification passage and the low temperature fluid in the evaporation passage causes the evaporation of the low temperature fluid and the formation of the mixed gas in the rectification passage. The rectification can be performed efficiently. Moreover, the lower portion of the rectification passage is adjacent to the dummy portion continuously provided below the evaporation passage, and in this portion, direct heat exchange with the fluid in the evaporation passage is not performed, and in the portion above this portion. Since the heat exchange is performed only between the rectification passage and the evaporation passage, the mixed gas in the rectification passage can be condensed only in the upper part and not in the lower part. Therefore, the entire height region of the rectification passage, that is, the height region required for rectification, is refined by gas-liquid contact without wasting the upper portion of the rectification passage unlike the conventional device in which condensation starts at the lower portion of the rectification passage. It can be fully utilized as a distillation device, which has the effect of performing efficient and sufficient rectification.

Further, in the apparatus according to the second aspect of the present invention, the sub-evaporation passage is provided above the vaporization passage, and the heat is further exchanged between the sub-evaporation passage and the upper portion of the rectification passage. This heat exchange has the effect of further promoting the condensation of the gas in the rectification passage, and thereby further increasing the purity of the low boiling point component in the gas taken out from the rectification passage.

In the carbon monoxide cryogenic separation device according to claim 3, the evaporation passage is used as a reboiler of the rectification column, and heat is exchanged between the mixed gas and the bottom liquid in the evaporation device to perform the rectification. The mixed gas is rectified in the passage, and the high-purity rectified gas obtained by this is supplied to the top of the rectification column as a reflux liquid. By using the existing reboiler as a gas rectification means without using it or refluxing a part of the product gas, it is possible to efficiently generate a high-purity reflux liquid, and thereby at low cost. There is an effect that high-purity product CO gas can be obtained.

[Brief description of drawings]

FIG. 1A is a perspective view showing a state in which a reboiler according to an embodiment of the present invention is laid down, and FIG. 1B is a perspective view showing a state in which each port is removed from the reboiler.

FIG. 2 is an external front view of a reboiler in the cryogenic separation system.

FIG. 3 is a flow sheet of the reboiler.

4A is a cross-sectional view taken along line CC of FIG. 1B, FIG.
FIG. 3 is a sectional view taken along the line DD of FIG.

5 is a cross-sectional view taken along the line EE of FIG. 1 (b).

6 is a sectional view taken along line FF of FIG.

FIG. 7 is a flow sheet showing the overall configuration of a carbon monoxide cryogenic separation system including the reboiler.

FIG. 8 is a flow sheet of a reboiler in the second embodiment.

9A is a sectional front view showing an evaporation passage and a sub-evaporation passage in the reboiler, and FIG. 9B is a sectional front view showing a rectification passage in the reboiler.

FIG. 10 is a graph showing a temperature distribution in the reboiler.

FIG. 11 is a graph showing a temperature distribution in a conventional evaporation device.

[Explanation of symbols]

18 rectification tower 20 reboiler (evaporator) 32 mixed gas introduction pipe (mixed gas introduction passage) 38, 40, 42, 46 rectification gas transfer pipe (rectification gas transfer passage) 48 tower bottom liquid introduction pipe (bottom liquid) Introducing passage) 49 Gas recirculation pipe (gas recirculating passage) 59a Tower bottom liquid evaporation passage 59b Fractionation passage 62a Tower bottom liquid introduction port 62b Mixed gas introduction port 63a Evaporation gas outlet 63b Rectification gas outlet 68 Dummy part

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Hideyuki Kubota Inventor Hideyuki Kubota 2-3-1, Niihama, Arai-cho, Takasago-shi, Hyogo Kobe Steel Works Takasago Works (56) References Japanese Patent Publication No. 47-23161 (JP, B1)

Claims (3)

[Claims] 1. A plurality of evaporation passages extending vertically , having a liquid inlet at a lower portion and an evaporative gas outlet at an upper portion,
A dummy portion provided continuously below each evaporation passage, has a mixed gas inlet at the bottom, have a rectification gas outlet at the top, the
From the height of the lower end of the dummy part to the height of the upper end of the evaporation passage
With a plurality of rectification passages extending vertically to the position ,
The evaporation passage and the dummy part and the rectification passage are mutually watered.
Linked alternately disposed in a state adjacent to the horizontal direction, the steam
Fluid flowing in the generation passage and evaporation in the rectification passage
Heat exchange is performed between the passage and the fluid flowing in the adjacent portion , and this heat exchange causes condensation in the rectification passage.
The part where the liquid is adjacent to the dummy part in this rectification passage
Ascends this part while lowering the minute
The length of the evaporation passage, the dummy part, and the rectification passage.
The evaporation device is characterized in that the height is set . 2. The evaporation apparatus according to claim 1, wherein a sub-evaporation passage is provided above the evaporation passage in a state of being isolated from the evaporation passage, and the rectification passage is moved up to a position adjacent to the sub-evaporation passage. The evaporation device is configured so that heat exchange is performed between the fluid in the rectification passage and the fluid in the sub-evaporation passage. 3. Deep cooling of carbon monoxide, comprising a rectification column for separating carbon monoxide from a mixed gas containing at least carbon monoxide and hydrocarbons, and a reboiler for evaporating a bottom liquid of the rectification column. In the separation device, the evaporator of claim 1 or 2 is installed as the reboiler, and a bottom liquid introducing passage for introducing the bottom liquid of the rectification column into the evaporation passage from the liquid introducing port, and the evaporation A gas reflux passage for deriving the gas in the passage from the evaporative gas outlet and returning it into the rectification tower, and a mixed gas introduction passage for introducing a mixed gas from the mixed gas inlet into the rectification passage, A rectification gas transfer passage is provided for deriving the rectification gas rectified in the mixed gas passage from the rectification gas outlet of the rectification passage, and introducing the rectification gas into the top of the rectification tower as a reflux liquid. Characteristic deep-separation device for carbon monoxide.