JP5604677B2 - Separation apparatus for azeotropic mixture and method for separating azeotropic mixture - Google Patents

Description

  The present invention relates to an azeotrope separation apparatus and an azeotrope separation method. More specifically, the apparatus configuration and process are simple, so that the equipment cost can be kept low, the energy saving effect is high, and the azeotrope separation method and the azeotrope separation method can obtain a high purity component. About.

  Alcohols such as ethanol and isopropanol are obtained as a mixed aqueous solution containing water in the production process, but the alcohols in such a mixed aqueous solution have a low concentration, and there is a problem in making it as a product as it is. From such a problem, in order to obtain high-purity alcohols, dehydration is carried out by a separation step, but distillation separation is generally used for the dehydration operation in such a separation step, and a great deal of energy is consumed. It was supposed to be consumed. In addition, since alcohols having 2 or more carbon atoms such as ethanol and isopropanol form an azeotrope with water, in the distillation separation process, the alcohol is first concentrated to the azeotrope, and if further dehydration is required, An azeotropic distillation in which a third component such as an entrainer (also referred to as an azeotropic breaker) is added, dehydrated to concentrate alcohols is performed (see, for example, Patent Document 1). As an entrainer (azeotropic breaker) as the third component, for example, hexane, cyclohexane, benzene or the like is used.

  FIG. 2 is a schematic view showing an embodiment of a conventional azeotrope separation apparatus 100. The azeotropic mixture separation apparatus 100 shown in FIG. 2 includes three distillation columns 91 to 93, reboilers 94 to 96, a liquid-liquid separator 97, and coolers 98 and 99. The low-concentration isopropanol / water azeotrope produced from the reaction step is introduced into the first distillation column (azeotropic tower) 91, for example, concentrated to an azeotrope having an isopropanol concentration of about 85% by mass. . The azeotropic mixture obtained from the top of the distillation tower (azeotropic tower) 91 is sent to the second distillation tower (dehydration tower) 92 and dehydrated by an appropriate entrainer (azeotropic distillation). High-purity isopropanol is obtained from the bottom of the distillation column (dehydration column) 92. The entrainer and water at the top of the tower are condensed and then separated into liquids by a liquid-separator 97, and the aqueous phase after the liquid-separation is treated by a third distillation tower (drainage stripper) 93, Water contained in the azeotropic mixture is obtained from the bottom of the column.

JP 2002-255876 A

  On the other hand, the distillation separation alone consumes a great deal of energy, and the conventional separation apparatus described above requires a plurality of (three in FIG. 2) distillation columns as represented by the configuration shown in FIG. Therefore, the equipment cost is high. In particular, in the apparatus as shown in FIG. 2, the total energy input to the reboiler in the three distillation columns is very large, or the system containing the third component, the entrainer, is azeotropically distilled. Because it was necessary to collect the entrainer separately, this was also a means to consume a lot of energy. Furthermore, azeotropic distillation is not preferable because the process and equipment configuration are complicated, and there is a problem that impurities are introduced into the product and wastewater due to the introduction of the third component.

  In recent years, a self-heat regeneration type distillation process has been provided as a technique capable of reducing the energy of the distillation column. In this process, the distillate vapor obtained from the top of the distillation column is compressed by a compressor and used for preheating the heat source and raw material of the reboiler, thereby greatly reducing the total energy input in the existing distillation column. Is possible. On the other hand, when such a process is used as a process for distilling alcohols from a mixed system of alcohols such as isopropanol and water as described above, a similar energy reduction effect can be expected, but components obtained from the top of the column Remained an azeotrope of alcohols and water, and improvements were desired.

  The present invention has been made to solve the above-described problems, and the configuration and process of the apparatus are simple and low-cost, and the energy input can be reduced, so that the energy saving effect is high, and the purity of the obtained component An object of the present invention is to provide an apparatus for separating an azeotropic mixture and a method for separating the azeotropic mixture.

In order to achieve the above object, an apparatus for separating an azeotrope according to the present invention includes a distillation column for distilling an input azeotrope to obtain a distillate and a bottoms, and the distillate obtained. A branch part for branching into steam for the reboiler heat source (distilled steam A) and steam for product extraction (distilled steam B), a compressor for compressing and heating the distillate steam before branching , Alternatively , at least one of a pair of compressors for compressing and heating each of the distillate steam A and the distillate steam B after being branched, and the reboiler using the distillate steam A that has been compressed and heated as a heat source A path for supplying the distillate steam A that has passed through the reboiler, a path for returning the distillate steam A that has passed through the reboiler, and a steam that allows the distillate steam B that has been compressed and heated to pass through to be separated into a non-permeate component and a permeate component The permeable membrane and the non-permeable component separated by the vapor permeable membrane A path to be sent out as a heating means of the azeotropic mixture, a first output unit for outputting and collecting the non-permeate component, a second output unit for outputting and collecting the bottom liquid obtained by distillation, It is characterized by providing.

In the azeotrope separation apparatus according to the present invention, in the above-described present invention, the compressor compresses and raises the temperature of each of the distillate vapor A and the distillate vapor B after being branched. The set of compressors is compressed before the distillate vapor A after being branched is supplied to the reboiler and before the distillate vapor B passes through the vapor permeable membrane. It is arranged to increase the temperature.

  The apparatus for separating an azeotropic mixture according to the present invention is characterized in that, in the above-described present invention, a path for returning the permeated component separated by the vapor permeable membrane to the distillation column is provided.

  The apparatus for separating an azeotropic mixture according to the present invention is characterized in that, in the above-described present invention, the vapor permeable membrane is a zeolite membrane.

The method for separating an azeotrope according to the present invention includes a step of distilling an input azeotrope with a distillation column to obtain a distillate vapor and a bottom liquid, and the distillate obtained is used for a reboiler heat source. A step of branching into steam (distilled steam A) and product extraction steam (distilled steam B), a step of compressing and raising the temperature of the distillate before branching , or the distilling after branching Passing through the reboiler, at least one of the steps of compressing and raising the temperature of each of the outgoing steam A and the distilled steam B, supplying the compressed and heated hot steam A to the reboiler as a heat source, and Returning the distillate vapor A to the distillation column, passing the compressed and heated distillate vapor B through a vapor permeable membrane and separating the non-permeate component and the permeate component, and the vapor permeable membrane The non-permeate component separated by After heating means compounds, and recovering, characterized in that it comprises a step of collecting the bottom product obtained by the distillation.

In the method for separating an azeotropic mixture according to the present invention, in the above-described present invention, the step of compressing and raising the temperature compresses and raises the distillate vapor A and the distillate vapor B after being branched. And before the distillate vapor A after being branched is supplied to the reboiler and before the distillate vapor B passes through the vapor permeable membrane. It is characterized by being compressed and heated.

  The method for separating an azeotropic mixture according to the present invention is characterized in that, in the above-described present invention, the method comprises a step of returning the permeated component separated by the vapor permeable membrane to the distillation column.

  The method for separating an azeotropic mixture according to the present invention is characterized in that, in the above-described present invention, the vapor permeable membrane is a zeolite membrane.

  The method for separating an azeotrope according to the present invention is characterized in that, in the above-described present invention, the azeotrope comprises an alcohol having 2 or more carbon atoms and water.

  According to the present invention, the cost and equipment cost can be kept low because the configuration and process of the apparatus are simple, and the energy saving effect is high, and the components are separated using a vapor permeable membrane, so the purity is high. An apparatus for separating an azeotrope from which components are obtained and a method for separating an azeotrope can be provided.

It is the schematic which showed the one aspect | mode of the separation apparatus of the azeotropic mixture which concerns on this invention. It is the schematic which showed the one aspect | mode of the separation apparatus of the conventional azeotrope. It is the figure which showed the flowchart of an example of the separation method of the azeotrope which concerns on this invention.

(I) Configuration of azeotropic mixture separation device:
Hereinafter, the configuration of an embodiment of the azeotrope separation apparatus according to the present invention will be described with reference to FIG. FIG. 1 is a schematic view showing one embodiment of an azeotropic mixture separation apparatus according to the present invention. The azeotrope separation apparatus 1 (hereinafter sometimes referred to as “separation apparatus 1”) according to the present embodiment shown in FIG. 1 includes a distillation column 2, a branching section 3, a first compressor 41, and a second compression. The machine 42, the reboiler 5, the vapor permeable membrane 6, the first output unit 71, the second output unit 72, and the paths 80 to 90 are provided as basic configurations.

  Separation apparatus 1 according to the present invention comprises two components constituting an azeotrope (the first component is a component different from the first component, has a higher boiling point than the first component, and forms an azeotrope with the first component. Used to separate the second component). The target azeotrope combination is not particularly limited. For example, a combination of alcohol having 2 or more carbon atoms (ethanol, propanol, isopropanol, butanol, etc.) and water, an aromatic compound, alcohol, aromatic A combination of a family and paraffin can be mentioned.

  The distillation column 2 inputs an azeotropic mixture that is a raw material and is a separation target from the input unit 70. The azeotropic mixture to be separated is a first component (for example, an alcohol having 2 or more carbon atoms such as ethanol, isopropanol (IPA), butanol, etc.) and a component different from the first component. A mixed aqueous solution (fluid) containing a second component (for example, water) that forms a boiling mixture. The distillation column 2 separates the input azeotropic mixture into a distillate vapor containing the first component in the gaseous state and a bottom liquid composed of the second component in the liquid state. In the present embodiment, the preheater 11 is disposed between the input unit 70 and the distillation column 2, and the introduced raw material (azeotropic mixture) is preheated to an appropriate temperature. As the preheater 11, what uses well-known heating means, such as steam preheating, can be used, for example.

  The distillate vapor output from the distillation column 2 passes through the path 80 and reaches the branch part 3. In the branch portion 3, in this embodiment, the distillate vapor is branched into a reboiler heat source vapor (distillation vapor A) and a product extraction vapor (distillation vapor B). The proportion of distillate steam branching in the branch section 3 (ratio of distillate steam A and distillate steam B) is appropriately determined in consideration of the balance between the amount used as the heat source of the reboiler 5 and the amount extracted as the product. However, it is preferable that the distillate steam A (the amount used as the heat source of the reboiler 5) is approximately 1.2 to 2.0 times the minimum reflux ratio, preferably 1.2 to 1.5 times. A range is particularly preferred.

  Of the distillate vapor branched at the branching section 3, the distillate vapor A passes through the path 81 and is input to the first compressor 41. The first compressor 41 raises the temperature by compressing the input distillate vapor A so as to reach a temperature level at which heat exchange with the reboiler 5 is possible. As the 1st compressor 41, a screw type compressor, a turbo type compressor, etc. can be used, for example. The compression ratio of the first compressor 41 is preferably 1.5 to 5.0, for example, and the temperature when condensed in the reboiler 5 is 5 to 10 ° C. higher than the bottom temperature of the distillation column 2. It is preferable to set so that

  Distilled steam A compressed and heated by the first compressor 41 passes through the path 82 and is supplied to the reboiler 5. The reboiler 5 mainly heats the bottom of the distillation column 2. In this embodiment, the reboiler 5 is compressed as a heat source of the reboiler 5 by the first compressor 41 so that the temperature level is heat exchangeable with the reboiler. Since the heated distilled steam A can be used, it is not necessary to separately provide an external heating medium such as a boiler. Here, since the energy for heating with a heating medium such as a boiler is very large as compared with the energy for compressing the distillate steam A with the first compressor 41, in the present invention, the heating of the reboiler 5 is performed. It is possible to significantly reduce the energy required for energy saving, and energy saving can be achieved.

  The distillate vapor A that has passed through the reboiler 5 passes through the path 83 and is then introduced into the cooler 12 and cooled in order to prevent it from being reduced in pressure in the distillation column 2 and being flushed. Note that a valve (not shown) is provided in the path 83 so that the pressure of the distillate steam A passing through the path 83 is adjusted (lowered) to be approximately the same as that of the distillate steam passing through the path 80. May be. The distilled steam A cooled by the cooler 12 passes through the path 84 and is returned to the distillation column 2 again.

  On the other hand, the distillate steam B branched at the branching section 3 passes through the path 85 and is input to the second compressor 42. The second compressor 42 compresses and raises the temperature of the distillate steam B so that the raw material (azeotrope) introduced from the input unit 70 can be preheated. The compression ratio in the second compressor 42 is preferably, for example, 1.5 to 5.0, and the temperature of the distilled steam B is set to 10 to prevent condensation of steam inside the vapor permeable membrane 6. It is preferable to raise the temperature by 50 ° C.

  The distillate vapor B compressed and heated by the second compressor 42 passes through the path 86 and is introduced into the vapor permeable membrane 6 and passes through the vapor permeable membrane 6. The vapor permeable membrane 6 (also referred to as a vapor permeable separation membrane) permeates and takes out the vapor component (permeated component), separates the remaining component (non-permeated component), and sends it out to the path 88. In the separation device 1 according to the present embodiment, the vacuum pump 13 is disposed in the passage 87 on the permeation side of the vapor permeable membrane 6, and the permeation side is depressurized. Such a vacuum pump 13 creates a pressure difference between the introduction side (path 86 side) and the permeation side (path 87 side) of the vapor permeable membrane 6, and this pressure difference is used as a driving force according to the selection characteristics of the vapor permeable membrane 6. It is possible to preferentially permeate components that become vapor.

  The type of the vapor permeable membrane 6 may be determined as appropriate depending on the types of components constituting the azeotrope and the various conditions such as the temperature and pressure of the distillate introduced, and may be, for example, an organic (polymer) type. For example, if a polyimide film, a polyvinyl alcohol film, a cellulose acetate film, etc. are inorganic, a zeolite film, a carbon film, a ceramic porous film, etc. are mentioned. For example, when water is contained as a component constituting the azeotrope, a water vapor permeable membrane that selectively permeates water (water vapor) and can be efficiently separated from other components is used. be able to. In particular, when the azeotrope is a two-component system of alcohol and water having two or more carbon atoms, such as isopropanol and ethanol, the zeolite membrane, polyimide membrane, etc. that permeates water (water vapor) and separates from isopropanol, etc. are vaporized. It can be used as a permeable membrane and can be separated from an azeotropic mixture of isopropanol or the like and water by efficiently and selectively permeating water.

  The configuration (mesh diameter, shape, porous / non-porous, etc.) of the vapor permeable membrane 6 is not particularly limited. Like the types of the vapor permeable membrane 6, the types of components constituting the azeotrope and the introduction thereof What is necessary is just to determine suitably by various conditions, such as the temperature of the distillate steam B to be performed, and a pressure. Further, the vapor permeable membrane 6 may be used in the form of a so-called separation membrane module having a multi-tube type.

  Of the components separated by the vapor permeable membrane 6, non-permeate components (for example, isopropanol when the azeotropic mixture is a two-component system of isopropanol and water) are sent to the input unit 70 through the path 88, It is used as a heating means for preheating the azeotropic mixture. Since the raw material is preheated by such components, the load on the preheater 11 can be reduced, and the amount of heat required by the reboiler 5 can be reduced. After passing through the input unit 70, the non-transmission component is output from the first output unit 71 to the outside of the system and is collected.

  On the other hand, among the components separated by the vapor permeable membrane 6, the permeable component (for example, water in the case where the azeotropic mixture is a two-component system of isopropanol and water) depends on the degree of selective characteristics of the vapor permeable membrane 6. In some cases, a non-transparent component (first component) is included. In the separation device 1 according to the present embodiment, the condenser 14 and the pump 15 for condensing the permeated component (steam) are disposed in the path 89 through which the permeated component (steam) passes, and the condenser The permeated component condensed at 14 etc. is returned to the distillation column 2 again.

  In addition, the bottomed liquid composed of the second component in a liquid state containing almost no first component separated by the distillation column 2 passes through the path 90 connected to the bottom of the distillation column 2 and is then output to the second output unit. The data is output from the system 72 and collected. A part of the bottoms discharged out of the system is heat-exchanged by the reboiler 5.

(II) An example of a method for separating an azeotropic mixture:
Hereinafter, the azeotrope separation method using the azeotrope separation apparatus 1 according to the present embodiment is an azeotrope of isopropanol (IPA) and water as an azeotrope to be separated. An example is given and demonstrated using the flowchart shown in FIG.

  First, an azeotropic mixture composed of isopropanol (first component) and water (second component) is input from the input unit 70, preheated by the preheater 11, and then input to the distillation column 2 (step 1 / S1). In the distillation column 2, the input azeotrope is separated into a distillate vapor containing the first component in the gaseous state and a bottom liquid composed of the second component in the liquid state (step 2 / S2). Distilled steam is output from the top of the tower.

  The distillate vapor output from the distillation column 2 is branched into reboiler heat source vapor (distillation vapor A) and product extraction vapor (distillation vapor B) (step 3 / S3). Of the distillate distillate, the distillate vapor A is compressed and heated by the first compressor 41 so as to reach a temperature level that allows heat exchange with the reboiler 5 (step 4 / S4). The heated distilled steam A is supplied to the reboiler 5 and used as a heat source for reboiler heating (step 5 / S5). Distilled steam A that has passed through the reboiler 5 is introduced into the cooler 12 and cooled. The distilled steam A cooled by the cooler 12 is returned again to the distillation column 2 (step 6 / S6).

  On the other hand, the distillate steam B branched in the branch section 3 is compressed and heated by the second compressor 42 so that the raw material (azeotrope) introduced from the input section 70 can be preheated. (Step 7 / S7). The distillate vapor B compressed and heated by the second compressor 42 is input to the vapor permeable membrane 6 and separated into a non-permeate component (isopropanol: first component) and a permeate component (water: second component) ( Step 8 / S8). In addition, by providing a pressure reducing means such as a vacuum pump 13 on the permeation side of the vapor permeable membrane 6, the permeation side is depressurized, so that a pressure difference can be generated between the introduction side and the permeation side of the vapor permeable membrane 6. By using this pressure difference as a driving force, it is possible to preferentially permeate the component that becomes the vapor according to the characteristics of the vapor permeable membrane 6.

  Of the components separated by the vapor permeable membrane 6, the non-permeable component (isopropanol: first component) is sent to the input unit 70 and supplied / utilized as a heating means for preheating the raw material (step 9 / S9). After passing through the input unit 70, the non-transmission component is output from the first output unit 71 to the outside of the system and collected (step 10 / S10). On the other hand, among the components separated by the vapor permeable membrane 6, the permeated component (water: second component) is preferably condensed and then returned to the distillation column 2 again (step 11 / S11). The non-permeable component (first component) that may be contained is recovered again.

  In addition, the bottoms of the second component in the liquid state, which is substantially free of the first component, separated by the distillation tower 2 is output from the second output unit 72 to the outside of the system from the bottom of the distillation tower 2 and recovered. (Step 12 / S12). A part of the bottoms discharged out of the system is heat-exchanged by the reboiler 5.

  According to the azeotrope separation apparatus 1 and the separation method according to the present invention described above, when the azeotrope is separated into constituent components, the distillate vapor from the distillation tower 2 is converted into the reboiler heat source vapor (distillation). Steam A) is divided into product extraction steam (distilled steam B), and the reboiler heat source steam is compressed and heated and used as the reboiler heat source, so a heating medium for heating the reboiler 5 is separately provided. There is no need to dispose it, and so-called self-heat regeneration type distillation can be performed to save energy.

  Further, by compressing and raising the temperature of the product extraction steam and separating it with the vapor permeable membrane 6, the component to be separated can be selectively separated, and the third component (entrainer) used in the existing process can be separated. , An azeotropic distillation using an azeotropic breaker is not required, and a high-purity component with few impurities can be obtained.

  Furthermore, since the distillate vapor path of so-called self-heat regeneration type distillation is improved and this is combined with the vapor permeable membrane 6, an operation for separately collecting a plurality of distillation columns 2 and third components is also required. In addition, the existing distillation separation process can be simplified.

  The aspect described above shows one aspect of the present invention, and the present invention is not limited to the above-described embodiment, and has the configuration of the present invention and can achieve the objects and effects. It goes without saying that modifications and improvements within the scope are included in the content of the present invention. Further, the specific structure, shape, and the like in carrying out the present invention are not problematic as other structures, shapes, and the like as long as the objects and effects of the present invention can be achieved. The present invention is not limited to the above-described embodiments, and modifications and improvements within the scope that can achieve the object of the present invention are included in the present invention.

  For example, in the above-described embodiment, the distillate vapor from the distillation column 2 is branched into the reboiler heat source vapor (distillation vapor A) and the product extraction vapor (distillation vapor B) at the branch section 3, and the reboiler 5. The first compressor 41 is disposed between the path 81 and the path 82 before being supplied to the gas to compress and heat the distillate vapor A, and the path 85 and path 86 before passing through the vapor permeable membrane 6 A mode in which the second compressor 42 is disposed between them to compress and heat the distilled steam B is shown. On the other hand, the position of compression of distillate steam (distillation steam A, distillate steam B) and the number of compressors are not limited to this, and instead of the first compressor 41 and the second compressor 42, for example, 1, a compressor is disposed in the path 80 of FIG. 1, the distillate vapor from the distillation column 2 is compressed and heated, and is branched into distillate A and distillate B at the branch section 3. A may be supplied to the reboiler 5 and the distillate vapor B may be introduced into and passed through the vapor permeable membrane 6. In addition, the distillate steam before branching is compressed and heated in this way, and then branched into the distillate steam A and the distillate steam B at the branch section 3. For example, before the distillate steam A is supplied to the reboiler 5. The first compressor 41 is disposed between the path 81 and the path 82, and the second compressor 42 is disposed between the path 85 and the path 86 before the distillate vapor B passes through the vapor permeable membrane 6, for example. The distillate steam A and the distillate steam B are further compressed and heated so that the distillate steam A is supplied to the reboiler 5 and the distillate steam B is introduced into and passed through the vapor permeable membrane 6. It may be.

In the above-described embodiment, the permeated component separated by the vapor permeable membrane 6 is returned to the distillation column 2 again through the path 89. However, there is a case where the separation performance of the vapor permeable membrane 6 is sufficient. Thus, the permeated component may be recovered outside the system without returning to the distillation column 2.
In addition, the specific structure, shape, and the like in the implementation of the present invention may be other structures as long as the object of the present invention can be achieved.

  EXAMPLES Hereinafter, although this invention is demonstrated further in detail based on an Example and a comparative example, this invention is not limited to this Example etc. at all.

[Example 1 and Comparative Example 1]
As the azeotrope, isopropanol and water (content of isopropanol with respect to the whole azeotrope at the time of input: 87.1% by mass, water content: 12.9% by mass) are shown in FIG. 1 (Example 1) and FIG. The separation apparatus shown in Example 1) was subjected to the separation operation of the azeotrope, and compared and evaluated.

  The basic conditions of the distillation column and the compressor in Example 1 and Comparative Example 1 are as follows, and the distillation column is made of SUS304 in both Example 1 (FIG. 1) and Comparative Example 1 (FIG. 2). This is a distillation column. Table 1 (Example 1) and Table 2 (Comparative Example 1) show the temperature, pressure, flow rate, and isopropanol and water composition at AK in FIG. 1 and af in FIG. Table 3 shows a comparison of the total energy (heat amount) used by both.

(Device specifications: Example 1)
Distillation tower 2: tower diameter 100 mm, height 20 m, packing SUS304 5/8 ball ring first compressor 41, second compressor 42: reciprocating type steam compressor steam permeable membrane 6: zeolite membrane (diamembrane / (Mitsubishi Chemical Corporation)

(Device specifications: Comparative example 1)
Distillation tower (azeotropic tower) 91: tower diameter 100 mm, height 20 m, packed 5/8 ball ring made of SUS304 Distillation tower (dehydration tower) 92: tower diameter 50 mm, height 20 m, packed 5/8 ball made of SUS304 Ring Distillation tower (drainage stripper) 93: tower diameter 50 mm, height 20 m, packing 5/8 ball ring made of SUS304 Compressor 94-96: Reciprocating type steam compressor Entrainer types: hexane, cyclohexane, benzene

(Result: Example 1)

(Result: Comparative Example 1)

(Comparison of total energy used)

  As shown in Table 1, when the separation method using the apparatus according to the present invention shown in FIG. 1 was used, isopropanol and water having a purity of almost 100% could be obtained. Further, as shown in Table 3, when the separation method is used by the apparatus according to the present invention shown in FIG. 1, the total energy input amount is compared with the distillation separation method using the conventional apparatus shown in FIG. It was confirmed that it was possible to suppress the value to about 1/5.

  The present invention can be advantageously used as a means for separating high-purity alcohols from an azeotropic mixture of alcohols having 2 or more carbon atoms, such as ethanol and isopropanol, and water.

DESCRIPTION OF SYMBOLS 1 ... Separation apparatus of azeotrope 11 ... Preheater 12 ... Cooler 13 ... Vacuum pump 14 ... Condenser 15 ... Pump 2 ... Distillation tower 3 ... Branch part 41 ... 1st compressor 42 ... 2nd compressor 5 ... Reboiler 6 ... Steam permeable membrane 70 ... Input part 71 ... First output part 72 ... Second output part 80-90 ... Path

Claims (9)

A distillation column for distilling the input azeotrope to obtain distillate vapor and bottoms;
A branching portion for branching the obtained distilled steam into steam for a reboiler heat source (distilled steam A) and steam for extracting a product (distilled steam B);
At least a compressor for compressing and heating the distillate steam before branching , or a set of compressors for compressing and heating each of the distillate steam A and distillate steam B after branching On the other hand,
A path for supplying the distilled steam A that has been compressed and heated to a reboiler as a heat source;
A path for returning the distillate vapor A that has passed through the reboiler to the distillation column;
A vapor permeable membrane that passes the compressed, heated distillate vapor B and separates it into a non-permeable component and a permeable component;
A path for sending out the non-permeate component separated by the vapor permeable membrane as a heating means of the input azeotrope;
A first output unit that outputs and collects the non-transmissive component;
A second output unit for outputting and recovering the bottoms obtained by distillation;
An apparatus for separating an azeotropic mixture, comprising: The compressor includes a set of compressors for compressing and heating each of the distillate steam A and the distillate steam B after the branching;
The set of compressors compresses and heats up before the distillate vapor A after being branched is supplied to the reboiler and before the distillate vapor B passes through the vapor permeable membrane. The azeotropic mixture separation device according to claim 1, wherein the azeotropic mixture separation device is provided.   The apparatus for separating an azeotropic mixture according to claim 1, further comprising a path for returning the permeated component separated by the vapor permeable membrane to the distillation column.   4. The apparatus for separating an azeotropic mixture according to claim 1, wherein the vapor permeable membrane is a zeolite membrane. A step of distilling an input azeotrope with a distillation column to obtain distilled steam and bottoms;
Branching the obtained distillate steam into a reboiler heat source steam (distillation steam A) and a product extraction steam (distillation steam B);
Compressing and heating the distillate steam before branching , or compressing and heating each of the distillate steam A and distillate steam B after branching ; and
Supplying compressed and heated distillate vapor A as a heat source to a reboiler;
Returning the distillate vapor A that has passed through the reboiler to the distillation column;
Passing the compressed and heated distillate vapor B through a vapor permeable membrane and separating it into a non-permeable component and a permeable component;
Recovering the non-permeated component separated by the vapor permeable membrane after being used as a heating means for the input azeotrope;
Recovering the bottoms obtained by the distillation;
A method for separating an azeotropic mixture, comprising: The step of compressing and raising the temperature includes the step of compressing and raising the temperature of the distillate vapor A and the distillate vapor B after being branched,
By the compression and heating step, the distillate vapor A after being branched is compressed and heated before being supplied to the reboiler and before the distillate vapor B passes through the vapor permeable membrane. The method for separating an azeotropic mixture according to claim 5.   The method for separating an azeotropic mixture according to claim 5, further comprising a step of returning the permeated component separated by the vapor permeable membrane to the distillation column.   The method for separating an azeotropic mixture according to any one of claims 5 to 7, wherein the vapor permeable membrane is a zeolite membrane.   The method for separating an azeotrope according to any one of claims 5 to 8, wherein the azeotrope comprises an alcohol having 2 or more carbon atoms and water.

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