JP4220345B2 - Heat exchange apparatus using tower top vapor and tower bottom liquid and heat exchange method thereof - Google Patents

Description

The present invention relates to a heat exchange apparatus using a tower top vapor and a tower bottom liquid of a distillation tower and a heat exchange method thereof.

Generally, the heat exchanger in the distillation apparatus is used for the partial condensation of the top vapor of the tower, the heating of the liquid at the bottom of the tower, the heating or cooling of the distillation process substance moving between the distillation towers, and the entry / exit of the raw material, product substance or waste liquid into the distillation apparatus. There is a thing in each process like the heating or cooling in, and usually the tower top vapor is condensed by the condenser.

As an indirect heating source for exchanging heat with the distillation process substance, an internal heat exchange type distillation column for exchanging heat between the top vapor (product vapor) and the raw material liquid has been proposed.
Japanese Patent No. 3184501

Currently, in the heat exchange between the overhead steam and distillation process substance in the middle distillation stage, the top steam is fractionated to separate the high-boiling impurity component and low-boiling impurity component to obtain product components, and the distillation process substance is heated. Development of a specific apparatus or method to be carried out is desired.

Although the tower top vapor is condensed by the raw material liquid and heated by heating the raw material liquid (one of the distillation process substances) by an apparatus such as the internal heat exchange distillation column of the above-mentioned Japanese Patent No. 3184501, the heat can be recovered. The overhead vapor is totally condensed by a single stage heat exchange means, so this apparatus is used when separating high-boiling impurity components or low-boiling impurity components based on product components from the overhead vapor in the middle stage of distillation. It was difficult.

Furthermore, it is easy to solve the problem of obtaining a product component by separating the high-boiling impurity component and the low-boiling impurity component by separating the high-boiling impurity component with respect to the heat exchange between the overhead vapor in the intermediate distillation process and the distillation process substance. An effective improvement means has not been found so far.

In order to solve such problems, by exchanging heat between the tower top vapor and the liquid at the bottom of the tower flowing out from at least two distillation tower bottoms, the tower top steam is appropriately divided (boiling point) by each heat exchange. In order to stabilize the distillation operation of the entire distillation apparatus from the raw material containing different components, the ideal ratio of condensate rich in high-boiling components and steam rich in low-boiling components is referred to as “appropriate” ”) And the liquid at the bottom of each column is heated, resulting in energy saving and high quality products (products that have been subjected to proper partial reduction to remove impurities, Hereinafter, a heat exchange device and a heat exchange method capable of producing “high quality products”) were studied.

That is, the invention of the heat exchange device according to claim 1 is characterized in that the top steam is separated into gas and liquid in two stages of the first stage heat exchanger and the second stage heat exchanger, and the bottom of one distillation tower The column bottom liquid flowing out from the first stage heat exchanger is supplied to the first stage heat exchanger, and the column bottom liquid flowing out from the other one distillation column bottom is supplied to the second stage heat exchanger, respectively. In the heat exchange device,
The liquid at the bottom of the column flowing out from the bottom of one distillation column is supplied to the first stage heat exchanger, and the liquid at the bottom of the column flowing out from the bottom of the other distillation column is supplied to the second stage heat exchanger. A first stage heat exchanger cooling means and a second stage heat exchanger cooling means are provided so as to return to the bottom of the distillation column,
The first stage heat exchanger heating means in which the top vapor is supplied to the first stage heat exchanger from the top of the distillation tower, and the gas that has not been condensed in the first stage heat exchanger is the first stage heat exchanger The second stage heat exchanger heating means supplied to the second stage heat exchanger is provided.

The invention of the heat exchange device according to claim 2 is any one of the tower bottom liquid flowing out from the bottom of two or more distillation towers while the top vapor is separated into gas and liquid by two or more stages of heat exchangers. The two or more tower bottom liquids are branched by the combination of the two or more tower bottom liquids and the heat exchanger supplied to any one of the two or more stage heat exchangers, and the two or more stage heat exchangers are used. In the heat exchange equipment of the distillation tower that is heated,
Two or more tower bottom liquids flowing out from two or more distillation tower bottoms are supplied to any one of two or more heat exchangers in combination with two or more tower bottom liquids and heat exchangers. In order to return to the distillation column bottom of the supply source after each of the tower bottom liquid is branched and supplied to the two or more stage heat exchangers, respectively, it is provided with two or more stage heat exchanger cooling means,
The first stage heat exchanger heating means in which the top vapor is supplied from the top of the distillation tower to the first stage heat exchanger, and the gas not condensed in the first stage heat exchanger reaches the final stage heat exchanger. A heat exchanger heating means is provided in which the gas that has not been condensed in the previous heat exchanger is supplied to the next heat exchanger.

In the invention of the heat exchange method of claim 3, the top vapor is separated into gas and liquid in two stages of the first stage heat exchanger and the second stage heat exchanger, and flows out from the bottom of one distillation tower. The column bottom liquid heated by being supplied to the first stage heat exchanger and the column bottom liquid flowing out from the other one distillation tower bottom being heated by being supplied to the second stage heat exchanger In the heat exchange method of the tower heat exchange device,
As an indirect cooling source, the column bottom liquid flowing out from the bottom of one distillation column is supplied to the first stage heat exchanger, and the column bottom liquid flowing out from the bottom of the other one distillation column is supplied to the second stage heat exchanger, respectively.
As an indirect heating source, the top vapor is supplied from the top of the distillation column to the first stage heat exchanger, and the gas that has not been condensed in the first stage heat exchanger is supplied to the second stage heat exchanger. Features.

According to the heat exchange method of the present invention, the top vapor is separated into a gas and a liquid by two or more stages of heat exchangers, and any one of liquids at the bottom of the tower flowing out from the bottoms of two or more distillation towers. The two or more tower bottom liquids are branched by the combination of the two or more tower bottom liquids and the heat exchanger supplied to any one of the two or more stage heat exchangers, and the two or more stage heat exchangers are used. In the heat exchanging method of the heat exchanging device of the distillation tower that is heated,
As an indirect cooling source, the liquid at the bottom of the tower flowing out from the bottoms of the two or more distillation towers is branched and supplied to two or more heat exchangers, respectively.
As an indirect heating source, the top steam is supplied from the top of the distillation tower to the first stage heat exchanger, and the gas that has not been condensed in the first stage heat exchanger reaches the final stage heat exchanger. The gas not condensed in the exchanger is supplied to the heat exchanger in the next stage.

According to the present invention, the fractionation of the top vapor and the heating of the liquid at the bottom of the tower can be carried out in the same heat exchanger and the partial vaporization of the top vapor can be carried out. It is possible to separate components and low-boiling impurity components to obtain product components, and as a result, it is possible to produce high-quality products and save energy.

Moreover, any one of the liquids at the bottom of the two or more stages as an indirect cooling source is supplied to any one of the heat exchangers of the two or more stages, and the top steam is supplied from the top of the distillation tower as the indirect heating source. When the gas that has not been condensed in the previous stage heat exchanger is supplied to the next stage heat exchanger until the gas that has not been condensed in the first stage heat exchanger reaches the final stage heat exchanger. Therefore, it is possible to select the optimal permutation from the choices of two or more heat exchanger permutations based on the difference in the heat exchange amount in each heat exchanger, so that the optimal heat exchange permutation is determined and the top of the tower It is also possible to perform appropriate partial reduction corresponding to the impurity content ratio of the vapor.

In the embodiment, the present invention is applied to a heat exchange device of an ethanol distillation column.
This heat exchange apparatus comprises at least two stages of partial condensation with respect to the top vapor of the distillation tower, means for heating the liquid at the bottom of the tower flowing out from at least two distillation tower bottoms, and at least two or more stages of heat exchange. The tower top vapor is separated into gas and liquid by this heat exchange device, and the tower bottom liquid flowing out from two or more distillation tower bottoms is heated.

The indirect cooling means shows two forms below.
As one form, the liquid at the bottom of the column flowing out from the bottom of one distillation column is supplied to the first stage heat exchanger, and the liquid at the bottom of the column flowing out from the bottom of the other distillation column is supplied to the second stage heat exchanger. After that, the first stage heat exchanger cooling means and the second stage heat exchanger cooling means each returning to the bottom of the distillation column of the supply source are provided.
As another mode, two or more of the tower bottom liquid and the heat exchanger that supply any one of the tower bottom liquid flowing out from the bottom of the distillation tower at two or more places to any one of the two or more heat exchangers With the combination, the two or more tower bottom liquids are supplied to the two or more heat exchangers, respectively, and then provided with two or more heat exchanger cooling means each returning to the distillation column bottom of the supply source.

The indirect heating means includes a first stage heat exchanger heating means in which the top steam is supplied from the top of the distillation tower to the first stage heat exchanger, and a gas not condensed in the first stage heat exchanger is the final stage heat. The heat exchanger heating means is provided in which the gas that has not been condensed in the previous stage heat exchanger up to the exchanger is supplied to the next stage heat exchanger.

By configuring in this way, it is possible to perform the partial condensation of the tower top vapor and the heating of the liquid at the bottom of the tower in the same heat exchanger and perform an appropriate partial reduction, resulting in high quality. Product production and energy savings can be achieved, and the heat exchanger has the functions of both a condenser used for partial condensation of the top vapor and a reboiler used for heating the liquid at the bottom of the tower. It is also possible to plan.

Hereinafter, Example 1 is demonstrated based on the flowchart of the heat exchange apparatus of FIG.
In FIG. 1, 1 is a first-stage heat exchanger, 2 is a second-stage heat exchanger, 3 is a distillation tower that generates top vapor, and 4 and 5 are distillation towers that discharge the bottom liquid from the bottom of the distillation tower. is there.

The heat exchangers 1 and 2 are multi-tube heat exchangers in which the multi-tubes are installed so as to be perpendicular to the flat ground. The heat exchange is performed in the multi-tubes, and the tower top vapor condensate liquid level generated by partial condensation is changed. The height of the heat exchange area between the tower top vapor and the liquid at the bottom of the tower is determined by setting the height to either level outside the multi-tube in the heat exchanger, and as a result, the heat exchange amount can be adjusted. (Not shown).

In the heat exchanger, the top steam is supplied to the outside of the multi-tube in the heat exchanger from the side of the heat exchanger above the top steam condensate, and the uncondensed gas is heated from the top of the heat exchanger. The liquid that has flowed out and condensed out of the exchanger flows out of the heat exchanger from the bottom of the heat exchanger. For this reason, even if a gas-liquid separator is not provided on the downstream side of the heat exchanger, appropriate partial reduction is possible.

The top vapor generated at the top of the distillation column 3 passes through the first stage heat exchanger heating means 11 to the first stage heat exchanger 1, and the liquid at the bottom of the tower flowing out from the bottom of the distillation column 4 is subjected to the first stage heat exchange. The first stage heat exchanger 1 is supplied to each of the first stage heat exchangers 1 through the cooler cooling means 13, and the heat exchange between the tower top steam and the tower bottom liquid is performed in the first stage heat exchanger 1. By this heat exchange, the top vapor is separated into a gas and a liquid, the gas is supplied to the second stage heat exchanger 2 through the second stage heat exchange heating means 12, and the liquid is supplied to the distillation tower 3 from the reflux means 17. While being refluxed, the liquid at the bottom of the column is heated and introduced as a gas into the distillation column 4 of the supply source.

The gas supplied to the second stage heat exchanger 2 through the second stage heat exchange heating means 12 flows out from the bottom of the distillation column 5 and passes through the second stage heat exchanger cooling means 14 to pass through the second stage heat exchanger 2. Heat exchange with the liquid at the bottom of the column. By this heat exchange, the supplied gas is separated into a gas and a liquid, the gas is supplied to the condenser 6 having a gas-liquid separator through the condenser heating means 20, and the liquid is refluxed from the reflux means 17 to the distillation column 3. Or while being supplied to the distillation column of the next process, the liquid at the bottom of the column is heated and introduced as a gas into the distillation column 5 of the supply source.

Thus, according to the heat exchange apparatus of Example 1, the partial vaporization of the tower top steam and the heating of the liquid at the bottom of the tower can be performed in the same heat exchanger and the partial vaporization of the tower top vapor is possible. As a result, it becomes possible to produce high-quality products and save energy.

Hereinafter, Example 2 is demonstrated based on the flowchart of the heat exchange apparatus of FIG.
In FIG. 2, reference numerals 1 to 5 are the same as those in FIG. The heat exchangers 1 and 2 are multi-tube heat exchangers and have the same structure and function as those of the first embodiment shown in FIG.

In Example 2, two heat exchange methods are possible. The two heat exchange methods will be described below.

As one of the two types, the tower top vapor generated at the top of the distillation tower 3 passes through the first stage heat exchanger heating means 11 and flows into the first stage heat exchanger 1 from the bottom of the distillation tower 4. The bottom liquid passes through the first stage heat exchanger cooling means 13, passes through the first stage heat exchanger cooling means 13 on the downstream side of the branch point 31 (the second stage heat exchanger cooling means 21 on the downstream side of the branch point 31). 1) is supplied to the first stage heat exchanger 1, and the first stage heat exchanger 1 performs heat exchange between the tower top steam and the tower bottom liquid. By this heat exchange, the top vapor is separated into a gas and a liquid, the gas is supplied to the second stage heat exchanger 2 through the second stage heat exchanger heating means 12, and the liquid is distilled from the reflux means 17. While being refluxed to the tower 3, the liquid at the bottom of the tower is heated and passes through the first stage heat exchanger cooling means 13 as a gas and the first stage heat exchanger cooling means 13 downstream from the branch point 37 (from the branch point 37). The downstream first stage heat exchanger cooling means 24 does not pass through.) It is introduced into the distillation column 4 of the supply source.

The gas supplied to the second stage heat exchanger 2 through the second stage heat exchanger heating means 12 flows out from the bottom of the distillation column 5, passes through the second stage heat exchanger cooling means 14, and is downstream from the branch point 33. The bottom liquid supplied to the second stage heat exchanger 2 passes through the second stage heat exchanger cooling means 14 (the first stage heat exchanger cooling means 22 downstream of the branch point 33 does not pass). And heat exchange. By this heat exchange, the supplied gas is separated into a gas and a liquid, the gas passes through the condenser supply means 20 and is supplied to the condenser 6 having a gas-liquid separator, and the liquid is supplied from the reflux means 17 to the distillation column 3. In addition, the liquid at the bottom of the column is heated and passed through the second-stage heat exchanger cooling means 14 as a gas to the second-stage heat exchanger cooling means 14 on the downstream side of the branch point 35. Street (the second-stage heat exchanger cooling means 23 downstream from the branch point 35 does not pass through) and is introduced into the distillation column 5 of the supply source.

As the other of the two types, the tower top vapor generated at the top of the distillation tower 3 passes through the first stage heat exchanger heating means 11 and flows into the first stage heat exchanger 1 from the bottom of the distillation tower 5. The bottom liquid passes through the first stage heat exchanger cooling means 14, passes through the first stage heat exchanger cooling means 22 downstream from the branch point 33 (the second stage heat exchanger cooling means 14 downstream from the branch point 33). After that, at the branch point 34, the first stage heat exchanger cooling means 13 is supplied to the first stage heat exchanger 1, respectively. In the first stage heat exchanger 1, the tower top steam and the tower bottom liquid are supplied. The heat exchange is performed. By this heat exchange, the top vapor is separated into a gas and a liquid, the gas is supplied to the second stage heat exchanger 2 through the second stage heat exchanger heating means 12, and the liquid is distilled from the reflux means 17. While being refluxed to the tower 3, the liquid at the bottom of the tower is heated and passes as gas through the first stage heat exchanger cooling means 13 and through the first stage heat exchanger cooling means 24 downstream from the branch point 37 (from the branch point 37. The downstream first-stage heat exchanger cooling means 13 does not pass through.) After that, at the branch point 38, the first-stage heat exchanger cooling means 14 is introduced into the supply source distillation column 5.

The gas supplied to the second stage heat exchanger 2 through the second stage heat exchanger heating means 12 flows out from the bottom of the distillation column 4, passes through the second stage heat exchanger cooling means 13, and is downstream from the branch point 31. Through the second stage heat exchanger cooling means 21 (the first stage heat exchanger cooling means 13 downstream of the branch point 31 does not pass), and then the second stage heat exchanger cooling means at the branch point 32. Heat exchange is performed with the tower bottom liquid supplied to the second stage heat exchanger 2 through 14. By this heat exchange, the supplied gas is separated into a gas and a liquid, the gas passes through the condenser supply means 20 and is supplied to the condenser 6 having a gas-liquid separator, and the liquid is supplied from the reflux means 17 to the distillation column 3. In addition, the liquid at the bottom of the column is heated and passed through the second-stage heat exchanger cooling means 14 as a gas to the second-stage heat exchanger cooling means 23 downstream from the branch point 35. (The second-stage heat exchanger cooling means 14 downstream from the branch point 35 does not pass), and then passes through the second-stage heat exchanger cooler 13 at the branch point 36 and is introduced into the supply distillation column 4 Is done.

In the flow diagram of the heat exchange device in FIG. 2, heat exchange in two stages of the first stage heat exchanger and the second stage heat exchanger is shown, but the heat exchanger can be three or more stages ( As the number of stages of the heat exchanger increases, the number of options for the distillation operation for performing proper partial contraction increases. In other words, since an optimal permutation can be selected from two or more heat exchanger permutation options based on the difference in the heat exchange amount of each heat exchanger, the optimal heat exchange amount permutation is determined. It is possible to perform appropriate partial reduction corresponding to the impurity content ratio of the top vapor. In this case, depending on the permutation calculation method, the number of options increases in two ways for the two-stage heat exchanger, six for the three stages, and 24 for the four stages.

As described above, in addition to the effects described in the first embodiment, the following effects are further added to the heat exchange device according to the second embodiment. That is, the above-mentioned ethanol raw material contains a plurality of impurities having a higher boiling point and lower boiling point than ethanol, and the content ratio varies due to the difference in the impurity content of the top vapor due to the difference when the raw material storage is switched. By selecting a combination of two or more tower bottom liquids and a heat exchanger in which any one of the tower bottom liquids flowing out from the bottom of the distillation tower is supplied to any one of two or more heat exchangers, The permutation of the appropriate amount of heat exchange as described above is determined, and it is possible to perform appropriate partial reduction corresponding to the impurity content ratio of the top vapor.

Hereinafter, Example 3 is demonstrated based on the flowchart of the heat exchange apparatus of FIG.
In FIG. 3, 1 or 2 is a first stage heat exchanger, 2 or 1 is a second stage heat exchanger (when 1 is a first stage heat exchanger, 2 is a second stage heat exchanger. When 2 is a first stage heat exchanger, 1 is a second stage heat exchanger.) 3 is a distillation column that generates top vapor, and 4 and 5 are distillation columns that drain liquid from the bottom of the distillation column. It is. The heat exchangers 1 and 2 are multi-tube heat exchangers and have the same structure and function as those of the first embodiment shown in FIG.

In Example 3, two heat exchange methods are possible. The two heat exchange methods will be described below.

As one of the two ways, the top vapor generated at the top of the distillation column 3 passes through the first stage heat exchanger heating means 18 and passes through the first stage heat exchanger heating means 11 at the branch point 39 (first stage). The stage heat exchanger heating means 15 does not pass through.) In the first stage heat exchanger 1, the column bottom liquid flowing out from the bottom of the distillation column 4 passes through the first stage heat exchanger cooling means 13 and the first stage heat. Each is supplied to the exchanger 1, and in the first stage heat exchanger 1, heat exchange between the tower top steam and the tower bottom liquid is performed. By this heat exchange, the top vapor is separated into a gas and a liquid, and the gas passes through the second stage heat exchanger heating means 12 at 40 branch points (the condenser supply means 19 does not pass). The liquid is supplied to the two-stage heat exchanger 2, and the liquid is refluxed to the distillation column 3 by the reflux means 17 (not introduced into the distillation column in the next step), and the liquid at the bottom of the column is heated to form a gas as the supply source distillation column. 4 is introduced.

The gas supplied to the second stage heat exchanger 2 through the second stage heat exchanger heating means 12 flows out from the bottom of the distillation column 5, passes through the second stage heat exchanger cooling means 14, and enters the second stage heat exchanger. Heat exchange with the column bottom liquid supplied to 2. By this heat exchange, the supplied gas is separated into a gas and a liquid, and the gas passes through the condenser supply means 20 at the branching point 41 (the heat exchanger heating means 16 does not pass). The liquid is supplied to the condenser 6 having a separator, and the liquid is refluxed to the distillation tower 3 from the reflux means 17 or supplied to the distillation tower in the next step, and the liquid at the bottom of the tower is heated and introduced as gas into the distillation tower 5 of the supply source. The

As the other of the two ways, the top vapor generated at the top of the distillation column 3 passes through the first stage heat exchanger heating means 18 and passes through the first stage heat exchanger heating means 15 at the branch point 39 (first stage). The stage heat exchanger heating means 11 does not pass through.) In the first stage heat exchanger 2, the column bottom liquid flowing out from the bottom of the distillation column 5 passes through the first stage heat exchanger cooling means 14 and the first stage heat. Each is supplied to the exchanger 2, and in the first stage heat exchanger 2, heat exchange between the tower top steam and the tower bottom liquid is performed. By this heat exchange, the top vapor is separated into a gas and a liquid, and the gas passes through the second stage heat exchanger heating means 16 at the 41 branch point (the condenser supply means 20 does not pass). The liquid is supplied to the two-stage heat exchanger 1, and the liquid is refluxed to the distillation column 3 from the reflux means 17 (not introduced into the distillation column in the next step), and the liquid at the bottom of the column is heated to form a gas as the supply source distillation column. 5 is introduced.

The gas supplied to the second stage heat exchanger 1 through the second stage heat exchanger heating means 16 flows out from the bottom of the distillation column 4, passes through the second stage heat exchanger cooling means 13, and the second stage heat exchanger. Heat exchange is performed with the liquid at the bottom of the column supplied to 1. By this heat exchange, the supplied gas is separated into a gas and a liquid, and the gas passes through the condenser supply means 19 at 40 branch points (the heat exchanger heating means 12 does not pass). The liquid is supplied to the condenser 6 having a separator, the liquid is refluxed to the distillation tower 3 from the reflux means 17 or supplied to the distillation tower of the next step, and the liquid at the bottom of the tower is heated and introduced as gas into the distillation tower 4 of the supply source. The

In the flow diagram of the heat exchange device in FIG. 3, heat exchange in two stages of the first stage heat exchanger and the second stage heat exchanger is shown, but the heat exchanger is similar to the second embodiment in FIG. It is possible to use three or more stages (not shown), and as the number of stages of the heat exchange device increases, options for distillation operation for performing proper partial contraction increase. In this case, depending on the permutation calculation method, the number of options increases in two ways for the two-stage heat exchanger, six for the three stages, and 24 for the four stages. From this, basically, in Example 2 and Example 3, it is possible to obtain the same effect with respect to an increase in the choices in the distillation operation for performing appropriate partial contraction.

That is, in Example 3, two or more tower bottom liquids and a heat exchanger in which any one of the tower bottom liquid flowing out from two or more distillation tower bottoms is supplied to any one of the two or more heat exchangers. By selecting the combination of the above, it is possible to determine that the permutation of two or more appropriate heat exchange amounts is determined, and that it is possible to perform appropriate partial reduction corresponding to the impurity content of the top vapor. Equivalent to Example 2.

The third embodiment adds the following effects in addition to the same effects as the second embodiment. That is, although Example 3 has the same effect in comparison with Example 2, it can reduce the necessary heat exchange means, and consequently can simplify the distillation operation. Become. Further, in the case of ethanol distillation, the bottom liquids flowing out from different distillation tower bottoms as in Example 2 are supplied to the same heat exchanger (for example, the bottom of the distillation tower 4 or 5 is fed to the first stage heat exchanger). The liquid is supplied alternately.) In the common part of the heat exchanger cooling means for different tower bottom liquid, any of the tower bottom liquid may be contaminated by impurities other than ethanol. Example 3 which does not have the possibility in the apparatus principle is superior in ethanol quality control.

The heat exchanger flow sheet using the tower top steam and tower bottom liquid of Example 1 is shown. The heat exchange apparatus flow sheet using the tower | column top steam and tower | column bottom part liquid of Example 2 is shown. The heat exchange apparatus flow sheet using the tower | column top steam and tower | column bottom part liquid of Example 3 is shown.

Explanation of symbols

1 First-stage heat exchanger (first-stage heat exchanger or second-stage heat exchanger in FIG. 3)
2 Second-stage heat exchanger (second-stage heat exchanger or first-stage heat exchanger in FIG. 3)
3 Distillation tower for generating top vapor 4 Distillation tower 5 for flowing out the liquid at the bottom of the tower 6 Distillation tower 6 for discharging the liquid at the bottom of the tower 6 Condenser 11 First-stage heat exchanger heating means 12 Second-stage heat exchanger heating means 13 First Stage heat exchanger cooling means (first stage heat exchanger cooling means or second stage heat exchanger cooling means in FIG. 2 or 3)
14 Second stage heat exchanger cooling means (second stage heat exchanger cooling means or first stage heat exchanger cooling means in FIG. 2 or FIG. 3)
15 First-stage heat exchanger heating means 16 Second-stage heat exchanger heating means 17 Reflux means 18 First-stage heat exchanger heating means 19 Condenser supply means 20 Condenser supply means 21 Second-stage heat exchanger cooling means 22 First Stage heat exchanger cooling means 23 Second stage heat exchanger cooling means 24 First stage heat exchanger cooling means 31 Branch point 32 Branch point 33 Branch point 34 Branch point 35 Branch point 36 Branch point 37 Branch point 38 Branch point 39 Branch Point 40 Branch point 41 Branch point

Claims (4)

The top steam is separated into gas and liquid in two stages, the first stage heat exchanger and the second stage heat exchanger, and the bottom liquid flowing out from the bottom of one distillation tower is the first stage heat exchanger. In the heat exchange apparatus of the distillation column, the column bottom liquid flowing out from the bottom of the other one distillation column is heated by being supplied to the second stage heat exchanger,
The liquid at the bottom of the column flowing out from the bottom of one distillation column is supplied to the first stage heat exchanger, and the liquid at the bottom of the column flowing out from the bottom of the other distillation column is supplied to the second stage heat exchanger. A first stage heat exchanger cooling means and a second stage heat exchanger cooling means are provided so as to return to the bottom of the distillation column,
The first stage heat exchanger heating means in which the top vapor is supplied to the first stage heat exchanger from the top of the distillation tower, and the gas that has not been condensed in the first stage heat exchanger is the first stage heat exchanger A heat exchange device, characterized in that a second-stage heat exchanger heating means supplied to the second-stage heat exchanger is disposed. The top vapor is separated into gas and liquid by two or more stages of heat exchangers, and any one of the column bottom liquid flowing out from the bottom of two or more distillation towers is one of two or more stages of heat exchangers. In a heat exchange apparatus for a distillation column in which two or more tower bottom liquids are branched by a combination of two or more tower bottom liquids supplied to one and a heat exchanger, and are heated using two or more heat exchangers, respectively. ,
Two or more tower bottom liquids flowing out from two or more distillation tower bottoms are supplied to any one of two or more heat exchangers in combination with two or more tower bottom liquids and heat exchangers. In order to return to the distillation column bottom of the supply source after each of the tower bottom liquid is branched and supplied to the two or more stage heat exchangers, respectively, it is provided with two or more stage heat exchanger cooling means,
The first stage heat exchanger heating means in which the top vapor is supplied from the top of the distillation tower to the first stage heat exchanger, and the gas not condensed in the first stage heat exchanger reaches the final stage heat exchanger. A heat exchanger apparatus characterized in that a heat exchanger heating means is provided in which the gas that has not been condensed in the previous stage heat exchanger is supplied to the next stage heat exchanger. The top steam is separated into gas and liquid in two stages, the first stage heat exchanger and the second stage heat exchanger, and the bottom liquid flowing out from the bottom of one distillation tower is the first stage heat exchanger. In the heat exchanging method of the heat exchanging device of the distillation column heated by being fed to the column, and the column bottom liquid flowing out from the bottom of the other one distillation column is fed to the second stage heat exchanger,
As an indirect cooling source, the bottom liquid that flows out from the bottom of one distillation column is supplied to the first stage heat exchanger, and the bottom liquid that flows out from the bottom of the other one distillation tower is supplied to the second stage heat exchanger, respectively.
As an indirect heating source, the top vapor is supplied from the top of the distillation column to the first stage heat exchanger, and the gas that has not been condensed in the first stage heat exchanger is supplied to the second stage heat exchanger. A heat exchange method for a heat exchange device. The top vapor is separated into gas and liquid by two or more stages of heat exchangers, and any one of the column bottom liquid flowing out from the bottom of two or more distillation towers is one of two or more stages of heat exchangers. A distillation column heat exchange apparatus in which two or more tower bottom liquids are branched by a combination of two or more tower bottom liquids and a heat exchanger supplied to one and heated by using two or more stages of heat exchangers, respectively. In the heat exchange method,
As an indirect cooling source, the liquid at the bottom of the tower flowing out from the bottoms of the two or more distillation towers is branched and supplied to two or more heat exchangers, respectively.
As an indirect heating source, the top steam is supplied from the top of the distillation tower to the first stage heat exchanger, and the gas that has not been condensed in the first stage heat exchanger reaches the final stage heat exchanger. A heat exchange method for a heat exchange device, characterized in that the gas that has not been condensed in the exchanger is supplied to a heat exchanger in the next stage.

Images