KR20120084822A - Efficient method of recovery, concentration, and dehydration of low-concentrated biochemical - Google Patents

Abstract

PURPOSE: A method for manufacturing biochemical is provided to minimize the energy from fermented liquid and to isolate the biochemical of high concentration. CONSTITUTION: A method for manufacturing biochemical comprises: a step of collecting biochemical from fermented liquid by microorganism fermentation(S1); a step of concentrating the biochemical through distillation column(S2); and a step of collecting the biochemical. The biochemical is collected by injecting the fermented liquid onto a separation film selected from inorganic film, polymeric film or a mixture thereof. The polymeric film is polydimethylsiloxane or poly(1-(trimethylsilyl)-1-propyne). The inorganic film is silicalite or Zeolite Sieve of Molecular porosity-5(ZSM-5).

Description

Efficient METHOD OF RECOVERY, CONCENTRATION, AND DEHYDRATION OF LOW-CONCENTRATED BIOCHEMICAL}

The present invention relates to a method for recovering, concentrating, and dehydrating a low concentration of biomass-derived chemicals at a high concentration while minimizing energy from fermentation broth.

In the biobutanol production technology, the recovery, concentration, and dehydration processes consume excessive energy and are known to make biobutanol difficult to commercialize. Specifically, the first problem in the recovery, concentration, and dehydration of biobutanol is that the concentration of the product in the fermentation broth is much lower than that of commercialized processes such as bioethanol, and the energy consumption is excessively high to recover it. As mentioned above, since azeotropes are formed with water, they cannot be separated from water through a general distillation process, and thus, a technology for effectively dehydrating water near the azeotropic point is required.

This problem is not only related to biobutanol, but also to most alcohols such as propanol, isopropanol and pentanol, which are high-end alcohols except for commercially available bioethanol. In addition, the same problem that the final fermentation concentration is low due to the low sugar concentration in the saccharified solution in the cellulosic (wood, herbal) biomass-based alcohol production technology, which can replace the raw material base of starch or sugar at present There is a need to develop a technology that can solve this problem.

Currently, the separation and purification process of commercially available bioethanol for fuel concentrates 90 wt% to 95 wt% of about 10 wt% ethanol through one or two distillation steps. Since ethanol forms azeotropes with water at a concentration of about 95% by weight, further water removal is achieved through an adsorption process using molecular sieves, finally producing more than 99.5% by weight of anhydrous ethanol.

The ethanol concentration of the fermentation broth produced in the dry milling corn ethanol process is 10 to 15% by weight, and 7 to 9% by weight for the sugarcane ethanol process. Based on this, the separation and purification energy in the dry mill cone ethanol process is about 4.5 MJ / kg, and in the case of sugarcane ethanol process, it is expected to be about 5 MJ / kg. However, when the concentration drops to 1 to 3% by weight, the required energy rises sharply above 20 MJ / kg. However, the concentration of biobutanol produced through the fermentation of biobutanol producing strains developed to date is up to 2% by weight, and at the same time, the total solvent concentration including ethanol and acetone is less than 3% by weight. It is much lower compared to the fermentation concentration of ethanol. The same is also true for other alcohol fermentations other than ethanol and bio-alcohol fermentation based on cellulose biomass. Therefore, in the case of low concentration of bio alcohol, there is a problem that excessive energy consumption is required when using the existing separation and purification process.

In addition, all alcohols except methanol in the C1 to C4 alcohols exhibit azeotropes with water. When azeotropes are formed, a new separation method is needed because separation is not possible by distillation, which is generally the most convenient way to separate mixtures. In the case of biobutanol, since n-butanol and ethanol, which form azeotropes with water, are generated at the same time, it is more difficult to simply apply the distillation process.

M. Matsumura et al. Calculated the energy of a separation and purification process consisting of decanters using the distillation process and the solubility of butanol in water. In the case of n-butanol, the solubility in water is 7.7g / 100mL (at 20 ° C), which is lower than the azeotropic point of water and n-butanol. Using this difference, this process designed a separation and purification process consisting of two columns (Water Column, Butanol Column) and decanter. Butanol, concentrated to a constant concentration in the distillation column, passes through a cooler and then enters the decanter. Since the introduced butanol concentration is above solubility, the decanter slowly separates into two layers, a butanol-rich layer (about 80 wt% butanol) and a water-rich layer (about 7.7 wt% butanol). The upper butanol-rich layer is further concentrated in the next butanol column, and the water-rich layer is refluxed to the distillation column.

The energy required to separate and purify up to 99.5 wt% butanol based on 1 wt% butanol is about 43 MJ / kg butanol, which is considered to be higher than the calorie content of butanol.

However, the process is limited to actually apply to bio butanol in that it is assumed that only water and n-butanol are present. In the biobutanol fermentation process, ethanol and acetone are simultaneously produced in addition to butanol, and since ethanol and acetone act as co-solvents to promote the dissolution of water and butanol, delamination in the decanter applied in the above process is prevented. It is unlikely to occur. Referring to the ternary phase equilibrium of Water-Butanol-Ethanol, it can be seen that no phase separation occurs for any composition of butanol and water when the ethanol concentration exceeds 20% by weight.

The Oak Ridge national Laboratory (ORNL) conducted a study on the development of a new separation and purification process considering the effects of phase separation prevention of ethanol and acetone. The proposed process was designed to counteract the effects of phase separation prevention of ethanol and acetone using methods that promote the phase separation effect by injecting additional salt into the fermentation broth. The process was compared to a commercial (distillation) process technique based on fermentation broth in 2% by weight solvent (ratio: 70% butanol, 3% ethanol, 27% isopropanol). In the case of a commercial process, since the phase separation does not occur in the composition of the solvent, it was simply configured by separating with concentration using a distillation column. However, this process did not achieve the ultimate energy savings. As a result of comparing the energy of the commercial process with the proposed process based on the design criteria, it was estimated that about 30 MJ / kg butanol was consumed in the commercial process and about 16 MJ / kg butanol in the proposed process. It is estimated that the proposed process can save about 40% of energy compared to the commercial process. However, considering that ethanol / water and IPA / water separation are not considered and both components form azeotropes with water, the proposed process would be expected to consume more than 20 MJ / kg of energy.

Therefore, the development of a new separation technology capable of effectively separating and dehydrating alcohols (butanol and ethanol, acetone (or isopropanol)) of 1 to 3% by weight in a fermentation broth while minimizing energy consumption is a next generation biotechnology including biobutanol. It is essential for the commercialization success of alcohol and cellulose biomass-based bio-alcohol.

In order to solve the above problems, the present invention comprises the steps of recovering the biochemical from the fermentation broth obtained by the microbial fermentation using biomass as a raw material; And it provides a method for producing a bio-chemical, comprising the step of dehydrating the recovered bio-chemical.

In one embodiment of the present invention, the step of concentrating through the distillation column may be further subjected to a step before the dewatering of the recovered biochemical.

In addition, as an embodiment of the present invention, the fermentation broth may be introduced into a separation membrane selected from a polymer membrane, an inorganic membrane, or a composite membrane thereof to recover the biochemical from the fermentation broth.

The fermentation broth may be heated to 40 ° C or more before being introduced into the separator, and the opposite side of the introduced separator may be maintained in a vacuum of 1 to 300 torr.

The polymer membrane may be polydimethylsiloxane or poly [1- (trimethylsilyl) -1-propyne], and the inorganic membrane may be silicalite or Zeolite Sieve of Molecular porosity-5 (ZSM-5).

In addition, in one embodiment of the present invention, it is possible to recover the biochemical from the fermentation broth using a steam stripper.

The biochemical may be recovered by steam, flowed out of the upper portion of the steam stripper into a vapor state, compressed, and then heat-exchanged with the effluent flowing out of the lower portion of the stripper.

Part of the effluent may be evaporated and reintroduced into the stripper by the heat exchange.

In addition, as an embodiment of the present invention, the recovered biochemical may be dehydrated by flowing into a separation membrane selected from a polymer membrane, an inorganic membrane or a composite membrane thereof.

The recovered biochemical is pressurized in a state of 1 to 10 bar (gauge pressure) to be introduced into the separator, and the opposite side of the introduced separator may be maintained at a vacuum of 1 to 350 torr.

The polymer membrane is at least one selected from the group consisting of polyvinyl alcohol, polyimide, polysulfone, polyamide, perfluoro-based polymer and chitosan, and the inorganic membrane is NaA zeolite (Zeolite · AAA), SiO ₂ day Can be.

In addition, as an embodiment of the present invention, the recovered biochemical may be dehydrated through an adsorption dehydration process passing through one or more adsorption towers containing an adsorbent.

The adsorption tower may include an adsorption tower for adsorbing moisture contained in the biochemical and an adsorption tower undergoing a regeneration process using a portion of the biochemical obtained through the adsorption tower as a purge gas.

The gas discharged from the adsorption tower undergoing the regeneration process may be recycled to the distillation column after condensation or vaporization.

The adsorbent may be a molecular sieve 3A (3A molecular sieve).

According to the present invention, in the production of biochemicals through microbial fermentation, biochemicals can be separated at a high concentration while minimizing energy from the fermentation broth.

1 is a process chart showing a manufacturing process in the method for producing a biochemical according to the present invention.
2 illustrates an apparatus in the case of recovering biochemicals using a steam stripper according to an embodiment of the present invention.
Figure 3 is a process chart showing the alcohol recovery, concentration and dehydration step in the method for producing a biochemical according to an embodiment of the present invention.
Figure 4 is a graph showing the result of recovering butanol from the fermentation broth using PDMS composite membrane as a recovery membrane.
Figure 5 is a graph showing the result when the dehydration process using a PVA-based polymer membrane as the dehydration membrane.
Figure 6 is a process chart showing the alcohol recovery, concentration and dehydration step in the method for producing a biochemical according to an embodiment of the present invention.

The present invention comprises the steps of recovering the biochemical from the fermentation broth obtained by the microbial fermentation using the biomass as a raw material; And it provides a method for producing a bio-chemical, comprising the step of dehydrating the recovered bio-chemical.

In the present invention, the term "biochemical" refers to a distillation column having higher volatility than water or a material that can be separated from water using a hydrophobic membrane because it has hydrophobic properties among chemicals produced by fermentation of microorganisms using biomass as a raw material. Means that can be separated into the upper portion, for example, alcohol (hereinafter referred to as bio alcohol) produced by the fermentation of microorganisms using biomass as a raw material, specifically biobutanol, bio ethanol, bio isopropanol and the like have,

The present invention provides a production method capable of separating biochemicals while minimizing energy from fermentation broth in the production of biochemicals through microbial fermentation. Particularly useful for the separation of bio butanol among biochemicals, but is not limited to bio butanol. Hereinafter, the bioalcohol will be described as an example of the biochemical.

In the manufacture of biochemicals using biomass as a raw material, the concentration of alcohol contained in the fermentation broth obtained by microbial fermentation using biomass as a raw material is generally 5% by weight or less, but according to one embodiment of the present invention. According to the method, the alcohol can be separated from the fermentation broth at a concentration of 99% by weight or more.

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1 is a process chart showing a manufacturing process in a method of manufacturing a biochemical according to an embodiment of the present invention.

Referring to Figure 1, the step of recovering alcohol from the fermentation broth obtained by the microbial fermentation using biomass such as wood-based material (S1); And dehydrating the recovered alcohol (S3), and may further include concentrating (S2) before dehydrating the recovered alcohol.

The alcohol recovered from the fermentation broth is butanol, isopropanol, ethanol, and the like, and may finally dehydrate water to 1% by weight or less through the dehydration process.

In the alcohol recovery, a separation membrane for recovery or a steam stripper may be used. In recovering alcohol such as butanol from the fermentation broth, when using a distillation column, there is a problem in that energy is excessively consumed in direct concentration to the azeotropic concentration of butanol.

In the case of using a recovery membrane in the recovery of alcohol (S1), the recovery separator selectively separates the alcohol to reduce the energy consumption while concentrating a low concentration of alcohol of 1 to 5% by weight to a concentration of 20% or more by weight. can do.

  The recovery separator may be a polymer membrane, an inorganic membrane, or a composite membrane of a polymer membrane and an inorganic membrane. The polymer membrane may be polydimethylsiloxane or poly [1- (trimethylsilyl) -1-propyne] (poly [1- (trimethylsilyl) -1-propyne]), and the inorganic membrane may be silicalite or zeolite. Sieve of Molecular porosity-5 (ZSM-5) can be used.

In order to increase the flux in the recovery membrane, the fermentation broth may be heated before flowing into the recovery membrane, and preferably, the temperature is raised to 40 ° C or higher. In order to facilitate separation in the recovery membrane, the opposite side of the recovery membrane into which the fermentation fluid is introduced may be maintained in a vacuum state. The vacuum is preferably maintained in the range of 1 to 300 Torr. The range of pressure and vacuum may vary depending on the characteristics of the recovery separator and the operating conditions.

The permeate separated through the recovery membrane enters the dehydration step or further concentration step in the vapor state, or after condensation enters the dehydration step or further concentration step.

2 illustrates an apparatus in the case of recovering biochemicals using a steam stripper according to an embodiment of the present invention.

Referring to FIG. 2, fermentation broth A containing alcohol at a low concentration of 1 to 5 wt% is introduced at the top of the steam stripper 210, and stripping steam B is placed at the bottom of the steam stripper 210. Inflow, the alcohol in the introduced fermentation broth (A) is recovered by the stripping steam (B).

When the concentration of the alcohol recovered from the upper end of the steam stripper 210 by the stripping steam (B) to the steam (C) state is less than 50%, after compressing the steam (C) with the compressor 220 After the alcohol is removed from the fermentation broth (A) by the stripping steam (B), the effluent (C) and the compressed steam (B) flowing out to the bottom of the steam stripper 210 are exchanged by the heat exchanger (230). Heat exchange converts the vapor into a liquid state. During the heat exchange process of the compressed steam (C) flow of the upper steam stripper 210 and the distillate (D) of the bottom of the steam stripper 210, some of the distillate (D) is evaporated and flows back into the steam stripper (210). Since the used steam is used as the stripping steam E, the amount of stripping steam required for the steam stripper 210 may be reduced. Compressed steam at the top of the steam stripper 210 is condensed through this process is converted into a liquid state and then introduced into a further concentration step (S2). The alcohol concentration in the influent F after the recovery step S1 is about 10 to 50% by weight.

When the concentration of the alcohol recovered in the steam (C) state at the top of the steam stripper 210 by the stripping steam (B) is 50% by weight or more, the heat exchange step with the effluent (D) at the bottom of the steam stripper 210 It may be introduced into the dehydration step (S3) without passing through.

After alcohol recovery, the concentration step S2 may use a distillation column. Alcohol concentrated to 10 to 50% by weight through the recovery step (S1) may be concentrated to 50 to 70% by weight through the concentration step (S2) as necessary. When the alcohol concentration after the recovery step (S1) is less than 20% by weight, it is preferable to go through the concentration step (S2) using a distillation column.

The reason for raising the alcohol concentration to 50 to 70% by weight through the recovery step and the further concentration step is that the azeotropic point is reached at about 50 to 60% by weight based on the ABE mixture due to the properties of butanol which form azeotropes with water. If it is no longer possible to separate the distillation column, and if the concentration is lower than this, the investment capacity is high due to the increased processing capacity of the membrane and adsorption tower system. Because it should be used as a level.

Dehydration step (S3) after the alcohol recovery (S1) or additional concentration step (S2) may use a membrane for dehydration, or may use an adsorbent.

According to one embodiment of the present invention, in the dehydration step (S3) it may be carried out according to the steam permeation process using the membrane for dehydration. In the alcohol recovery step S1 or the concentration step S2, the concentrated alcohol vapor is discharged through the overhead of the stripper or the distillation column and flows into the separator for dehydration. The introduced alcohol vapor is selectively separated and removed through a dehydration membrane, and finally dehydrated and concentrated to a concentration of 99% by weight or more of alcohol.

As the dehydration membrane, a single type of membrane may be used alone, or several types of membranes may be mixed and used, and a plurality of membranes may be used in stages as necessary. The membrane for dehydration may be selected from a polymer membrane, an inorganic membrane or a composite membrane thereof. The polymer membrane may be selected from the group consisting of polyvinyl alcohol, polyimide, polysulfone, polyamide, perfluoro, and chitosan. One or more kinds may be used, and as the inorganic membrane, NaA zeolite (Zeolite · NaA), SiO ₂ Etc. may be used.

The steam flowing into the dewatering separator may be pressurized using a compressor to increase the flux of the separator. That is, it may be pressurized to 1 to 10 bar (gauge pressure) before entering the dewatering separator. In addition, in order to facilitate the separation in the dewatering separator, the opposite side into which the steam flows in the separator may be maintained in a vacuum state, and may be preferably maintained in a vacuum of 1 to 350 torr. The range of pressure and vacuum may vary depending on the characteristics of the dehydration membrane and the operating conditions.

According to another embodiment of the present invention, the dehydration process may be performed according to the adsorption dehydration process using the adsorbent in the dehydration step (S3). In this case, an adsorbent capable of selectively adsorbing moisture may be used as the adsorbent, and preferably, 3A molecular sieve (3A) may be used.

The adsorption dehydration process using the adsorbent consists of passing through one or more adsorption towers containing an adsorbent capable of adsorbing water in the hydrous alcohol. The dehydration process can be carried out by using two or more adsorption towers. The concentrated hydrous alcohol vapor is branched into each adsorption tower. In one adsorption tower, the hydrous alcohol is introduced into the adsorption tower and the moisture of the hydrous alcohol is adsorbed. The adsorption tower of may be subjected to a regeneration process. Regeneration of the adsorption tower refers to a process of restoring the water adsorption performance through the dehydration process in the state where water is adsorbed. The regeneration of the adsorption column is generally carried out in a vacuum state, in which a portion of the anhydrous alcohol (for example, about 30%) is passed through the other adsorption tower and used as a purge gas to the adsorbent included in the regeneration adsorption tower. Consists of supplying. The adsorption and regeneration processes take place alternately and continuously. The gas discharged from the adsorption tower regenerated in the regeneration process may be vaporized or condensed and then recycled to a distillation tower to reduce energy and increase alcohol recovery.

The present invention will be described in more detail with reference to the following examples. However, the present invention is not limited to the following examples.

Example

Example  One

A computer based process simulator was used to evaluate the performance of the separation and dehydration process of butanol, acetone and ethanol from fermentation broth. The concentration of alcohol in the fermentation broth flowing into the separation and dehydration process was assumed to be 1.5% by weight, that is, 1.0% by weight of butanol, 0.2% by weight of acetone and 0.3% by weight of ethanol, and the final product (alcohol) was separated at a concentration of 99% or more. Assumed to be dehydration.

Figure 3 is a process chart showing the alcohol recovery, concentration and dehydration step in the method for producing a biochemical according to an embodiment of the present invention.

Referring to FIG. 3, a recovery membrane was used in a recovery step S1, a distillation column was used in a concentration step S2, and a membrane for dehydration was used in a dehydration step S3. As a recovery membrane, a composite membrane impregnated with silicalite in PDMS was used.

Figure 4 is a graph showing the result of recovering butanol from the fermentation broth using the PDMS composite membrane as a recovery membrane.

4, it was confirmed that 1% by weight of butanol was concentrated to about 15% by weight, and in the case of 1.5% by weight of alcohol, which is the feed composition of the present embodiment, it may be concentrated to a concentration of about 20% by weight. It is predicted.

Referring to FIG. 3 again, about 20% by weight of alcohol recovered using the separator is concentrated to about 60% by weight using an additional distillation column and flows out to the top of the distillation column. The 60% by weight alcohol vapor, which flowed out to the top of the distillation column, is finally dehydrated and concentrated to 99% by weight through the dehydration membrane, and the permeate through the dehydration membrane is condensed and recycled back to the distillation column.

60% by weight of the alcohol vapor flowing out of the distillation column was designed to be dehydrated using the alcohol dehydration membrane of the two stages, and after concentrating the alcohol to the concentration of about 85% by weight in the first stage, more than 99% by weight in the second stage Concentrated.

In the present embodiment, it is assumed that a polyvinyl alcohol (PVA) -based polymer membrane is used as the membrane for dehydration. An experiment is performed to determine the alcohol concentration in the permeate that has permeated through the membrane during dehydration using the membrane for dehydration. Was performed.

Figure 5 is a graph showing the result when the dehydration process using a PVA-based polymer membrane as a dewatering separator.

Referring to FIG. 5, the alcohol concentration in the permeate was found to be about 10-15 wt% while the 60 wt% alcohol mixture was concentrated to 99.5 wt%.

Based on the experimental results, the composition, conditions, and energy consumption of the main apparatus were estimated using the process simulator. The process scale was set to 40 kg / h based on the final product, and the composition of each calculated stream shown in FIG. 3 is shown in Table 1 below.

Referring to Table 1, the energy consumption of the process according to an embodiment of the present invention is calculated based on the load (Duty) of the heat exchanger (Reboiler) of the distillation column is about 92 MJ / hr, about 2.3 per kg of product It was calculated that the energy of MJ was consumed.

Example  2

A computer based process simulator was used to evaluate the performance of the separation and dehydration process of butanol, acetone and ethanol from fermentation broth. The concentration of alcohol in the fermentation broth flowing into the separation and dehydration process was assumed to be 1.5 wt%, that is, 1.0 wt% butanol, 0.2 wt% acetone and 0.3 wt% ethanol, and the final product (alcohol) was separated at a concentration of 99 wt% or more. , Dehydration was assumed.

6 is a process chart showing the alcohol recovery, concentration and dehydration step in the biofuel manufacturing method according to an embodiment of the present invention.

Referring to FIG. 6, a steam stripper was used in the recovery step S1, a distillation tower was used in the concentration step S2, and a separator for dehydration was used in the dehydration step S3.

Under atmospheric conditions, 1.5% by weight of alcohol was concentrated to about 17% by weight through a steam stripper and then flowed to the overhead of the stripper and compressed to 0.7 bar through a compressor. The compressed steam is condensed through the heat exchange process with the bottom of the stripper, and the recovered heat heats a portion of the bottom of the stripper to generate steam, and the generated steam is used as stripping steam.

About 17% by weight of alcohol recovered and condensed using the steam stripper was concentrated to about 60% by weight with an additional distillation column and flowed to the top of the column. 60% by weight of alcohol vapor flowing out of the column was finally dehydrated and concentrated to 99% by weight through the dehydration membrane, and the permeate passed through the dehydration membrane was condensed and recycled back to the concentration tower.

Based on the experimental results, the composition, conditions, and energy consumption of the main apparatus were estimated using the process simulator. The process scale was set to 40 kg / h based on the final product, and the composition of each calculated stream shown in FIG. 3 is shown in Table 2 below.

Referring to Table 2, the energy consumption of the process according to an embodiment of the present invention is calculated based on the load (Duty) of the heat exchanger (Reboiler) of the distillation column is about 240.4 MJ / hr, about 6 per kg product It was calculated that the energy of MJ was consumed.

Claims (15)

Recovering the biochemical from the fermentation broth obtained by the microbial fermentation using the biomass as a raw material; And
Dehydrating the recovered biochemical;
Method of producing biochemicals.
The method of claim 1,
The method of producing a biochemical, characterized in that further comprising the step of concentrating through a distillation column prior to the step of dehydrating the recovered biochemical.
The method of claim 1,
A method of producing a biochemical, wherein the fermentation broth is introduced into a separation membrane selected from a polymer membrane, an inorganic membrane or a composite membrane thereof to recover the biochemical from the fermentation broth.
The method of claim 3,
The fermentation broth is heated to 40 ℃ or more before entering the membrane, the biochemical manufacturing method, characterized in that to maintain the opposite side of the incoming membrane in a vacuum of 1 to 300 torr.
The method of claim 3,
The polymer membrane is polydimethylsiloxane or poly [1- (trimethylsilyl) -1-propyne], and the inorganic membrane is silica light or Zeolite Sieve of Molecular porosity-5 (ZSM-5).
The method of claim 1,
A method for producing biochemicals, comprising recovering biochemicals from fermentation broth using a steam stripper.
The method of claim 6,
The biochemical is recovered by steam, is discharged to the steam state in the upper portion of the steam stripper and compressed, and then heat exchanged with the effluent flowing out of the lower portion of the stripper.
The method of claim 7, wherein
And a part of the effluent is evaporated by the heat exchange and re-introduced into the stripper.
The method of claim 1,
The recovered biochemical is introduced into a separation membrane selected from a polymer membrane, an inorganic membrane or a composite membrane thereof to dehydrate.
10. The method of claim 9,
The recovered bio-chemical is pressurized to a state of 1 to 10 bar (gauge pressure) is introduced into the separator, the method of producing a bio-chemical, characterized in that to maintain the opposite side of the introduced separator in a vacuum of 1 to 350 torr.
10. The method of claim 9,
The polymer film is at least one selected from the group consisting of polyvinyl alcohol, polyimide, polysulfone, polyamide, perfluoro-based polymer and chitosan,
The inorganic membrane is NaA zeolite (Zeolite.NaA), SiO ₂ manufacturing method of the biochemical, characterized in that.
The method of claim 1,
A method of producing a biochemical, wherein the recovered biochemical is dehydrated through an adsorption dehydration process passing through one or more adsorption towers containing an adsorbent.
The method of claim 12,
The adsorption tower, biochemical production method characterized in that it comprises an adsorption tower for adsorbing the water contained in the biochemical and the adsorption tower undergoing a regeneration process using a portion of the biochemical obtained through the adsorption tower as a purge gas.
The method of claim 13,
The method of producing a biochemical, characterized in that for recycling the gas discharged from the adsorption column undergoing the regeneration process in a vapor state or after condensation to the distillation column.
The method of claim 12,
The adsorbent is a method for producing a biochemical, characterized in that the molecular sieve 3A (3A molecular sieve).

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