JP2012111725A - Apparatus for producing ethanol - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an apparatus for producing ethanol, which can smoothly and efficiently operate a distillation column system even when a fermented solution of a biomass is distilled.SOLUTION: The apparatus 1 for producing the ethanol includes: a fermentor 4 for fermenting a saccharified solution of the biomass; a distillator 5 for distilling the fermented solution obtained by the fermentor 4; and a carrier 43 for carrying the fermented solution from the fermentor 4 to the distillator 5. The carrier 43 includes on its way: a separator 44 for separating an inorganic compound contained in the fermented solution; and a filtering unit 45 for filtering, from the fermented solution, a protein contained in the fermented solution and the inorganic compound separated by the separator 44.

Description

  The present invention relates to an ethanol production apparatus.

  Conventionally, an ethanol production apparatus for producing bioethanol by saccharifying a substrate mixture obtained by mixing biomass with a solvent using a saccharification enzyme produced by a microorganism and fermenting the obtained saccharified solution is known. In the ethanol production apparatus, the fermentation solution obtained by fermentation of the saccharified solution is concentrated by distillation and further dehydrated, whereby ethanol having a concentration of, for example, about 99.9% by mass can be obtained (for example, Patent Document 1). reference).

  As one of the biomasses serving as the substrate, lignocellulosic biomass such as rice straw can be mentioned. The lignocellulosic biomass has a structure in which lignin is firmly bound to cellulose or hemicellulose. Therefore, by holding the substrate mixture at a predetermined temperature for a predetermined time, the lignin is dissociated from the substrate or the substrate is swollen to obtain a saccharification pretreatment product that enables saccharification of cellulose or hemicellulose. Enzymatic saccharification of processed products has been performed.

  In addition, in this application, dissociation means cut | disconnecting at least one part coupling | bonding among the binding sites of the lignin couple | bonded with the cellulose or hemicellulose of lignocellulosic biomass. Swelling means that voids are generated in cellulose or hemicellulose constituting crystalline cellulose by the intrusion of liquid, or voids are generated inside cellulose fibers to expand.

  In the ethanol production apparatus using the lignocellulosic biomass as a substrate, the saccharified solution is fermented with a fermentative bacterium or yeast to obtain the fermented solution. Depending on the performance of the fermented bacterium or yeast, the concentration of the fermented solution is 5 to 5. The concentration is as low as about 10% by mass. As a result, when the obtained fermentation solution is concentrated by distillation, there is a problem that heat energy increases. The energy required for ethanol concentration occupies a large weight of 30 to 50% of the energy required for the entire ethanol production process.

  In order to solve the above problem, it is indispensable to reduce thermal energy by increasing the efficiency of the ethanol concentration step in the ethanol production apparatus. Therefore, it is desired to efficiently distill the fermentation solution as one measure for reducing the thermal energy in the ethanol production apparatus.

JP 2010-65001 A

  However, when a distillation tower system is used as one method for concentrating ethanol in the fermentation solution obtained from the biomass, deposits adhere and accumulate in the distillation tower system, causing clogging of pipes, etc. There is an inconvenience that it may be disturbed.

  Therefore, the present invention has an object to provide an ethanol production apparatus that can eliminate such inconvenience and can smoothly and efficiently operate a distillation column system even when the fermentation solution obtained from the biomass is distilled. And

  To achieve this object, the ethanol production apparatus of the present invention comprises a fermentation means for fermenting a saccharified solution of biomass, a distillation means for distilling the fermentation solution obtained by the fermentation means, and the fermentation solution as the fermentation means. In the ethanol production apparatus comprising the transfer means for transferring from to the distillation means, the transfer means includes a separation means for separating an inorganic compound contained in the fermentation solution, a protein contained in the fermentation solution, and the separation on the way And a filtering means for filtering out the inorganic compound separated by the means from the fermentation solution.

  As a result of studying substances precipitated from the fermentation solution, the present inventors have found that the substance is an enzyme used for the saccharification, a complex of a protein derived from a fermenting bacterium or yeast cell used for the fermentation and an inorganic compound. I found out that it was a thing. As said inorganic compound, the inorganic compound as a component of the said biomass itself, the phosphate used for culture | cultivation of the said fermenting microbe or yeast, etc. can be considered.

  Based on the above knowledge, in the ethanol production apparatus of the present invention, first, the inorganic compound is separated by the separation means provided in the middle of the transfer means for transferring the fermentation solution from the fermentation means to the distillation means. Separation of the inorganic compound can be performed, for example, by adding a flocculant to the fermentation solution to aggregate the inorganic compound, or by adjusting the pH of the fermentation solution to precipitate the inorganic compound. .

  Therefore, in the ethanol production apparatus of the present invention, it is preferable that the separation means includes an addition means for adding a flocculant to the fermentation solution or an adjustment means for adjusting the pH of the fermentation solution.

  Next, in the ethanol production apparatus of the present invention, the protein contained in the fermentation solution and the inorganic compound separated by the separation means are filtered from the fermentation solution by a filtering means provided in the middle of the transfer means. To do. In order to efficiently separate the protein and the inorganic compound, the filtering means includes an inorganic compound filtering means for filtering the inorganic compound from the fermentation solution, and a downstream side of the inorganic compound filtering means. It is preferable to provide a protein filtration means for separating the protein from the fermentation solution.

  As the inorganic compound filtering means, for example, a filter having an opening in the range of 75 to 500 μm can be used. If the aperture of the filter is larger than 500 μm, the inorganic compound cannot be separated by filtration and may be mixed into the distillation means. In addition, if the mesh opening is smaller than 75 μm, the filter may be clogged and hinder the transfer of the fermentation solution. More preferably, the filter has an opening in the range of 150 to 250 μm.

  The protein filtration means preferably includes an ultrafiltration membrane having a molecular weight cut-off in the range of 1000 to 3500, or an ion exchange resin having a most frequent radius of 50 to 500 mm obtained by crosslinking acrylic or styrene with divinylbenzene.

  If the molecular weight cut off is greater than 3500, the ultrafiltration membrane may not be able to filter out the protein. Moreover, in order to make the said molecular weight cut off less than 1000, a more precise | minute filter membrane is required and the increase in cost may be unavoidable.

  When the most frequent radius exceeds 500 mm, the ion exchange resin may not be able to sufficiently filter proteins. Further, if the most frequent radius is less than 50 mm, the protein may pass through the surface of the ion exchange resin.

  According to the ethanol production apparatus of the present invention, since the protein and the inorganic compound are separated by the filtration means, it is possible to prevent deposits from adhering and accumulating in the distillation means, thereby making the distillation means smooth. Can be operated efficiently.

  Further, in the ethanol production apparatus of the present invention, the distillation means includes a first distillation column and a second distillation unit disposed inside the first distillation column and separated from the inside thereof. A distillation column, fermentation solution supply means for supplying the fermentation solution to the first distillation column, and gas supplied to the second distillation column by taking out the first gas obtained at the top of the first distillation column. A supply conduit, a pressure difference generating means provided in the middle of the gas supply conduit to make the pressure in the second distillation column higher than that in the first distillation column, and a first liquid for taking out the bottom liquid of the first distillation column An extraction conduit, a heating means for heating the first distillation column, a second extraction conduit for taking out the second gas obtained at the top of the second distillation column, and an intermediate portion of the second extraction conduit And a condenser for cooling and liquefying the second gas, and a second side wall of the second distillation column as the heat transfer surface. Preferably comprises a heat integrated distillation column to move the column of the heat to the first distillation column.

  In the internal heat exchange distillation column, first, the fermentation solution supplied to the first distillation column is heated and distilled by the heating means, so that the fermentation solution is added to the top of the first distillation column. A first gas containing a higher concentration of ethanol is obtained. The first gas is supplied to the second distillation column via the gas supply conduit. At this time, the pressure difference generating means causes the second distillation column to have a higher pressure than the first distillation column. As a result, the temperature in the second distillation column rises.

  In the internal heat exchange type distillation column, the pressure difference generating means is configured to set the first distillation column to atmospheric pressure, pressurize the first gas, and pressurize the second distillation column to atmospheric pressure or higher. It is good also as a state. Further, the pressure difference generating means may depressurize the inside of the first distillation column so that the inside of the first distillation column is in a reduced pressure state equal to or lower than atmospheric pressure, and the inside of the second distillation column may be set to atmospheric pressure.

  As a result, the first gas is further distilled in the second distillation column, and a second gas containing ethanol having a higher concentration than the first gas is obtained at the top of the second distillation column. The second gas is taken out from the second take-out conduit, cooled by the condenser, and liquefied, whereby an ethanol solution containing a higher concentration of ethanol than the fermentation solution can be obtained.

  Here, in the internal heat exchange type distillation column, the pressure in the second distillation column is set higher than that in the first distillation column by the pressure difference generating means, so that the temperature in the second distillation column is increased. The temperature rises and becomes higher than the temperature in the first distillation column. As a result, the heat of the second distillation column moves to the first distillation column using the side wall of the second distillation column as the heat transfer surface. Accordingly, the first distillation column is further heated, and the temperature of the second distillation column is lowered. Therefore, the heating and cooling work can be reduced, and the heat energy required for distillation can be reduced.

  However, in the internal heat exchange distillation column, when the deposit adheres and accumulates on the side wall of the second distillation column, which is a heat transfer surface, the precipitate acts as a heat insulating material, and thus heat transfer resistance increases. There is a concern that heat transfer from the second distillation column to the first distillation column is hindered.

  However, according to the ethanol production apparatus of the present invention, since the protein and the inorganic compound are separated from the fermentation solution by the filtration means, deposits are deposited on the side walls of the second distillation column. And the internal heat exchange distillation column can be operated smoothly. Therefore, when the distillation means includes the internal heat exchange distillation column, the thermal energy required for distillation can be further reduced.

  In the ethanol production apparatus of the present invention, for example, lignocellulosic biomass can be used as the biomass.

The system block diagram which shows the structure of the ethanol manufacturing apparatus of this invention. The chart of the Fourier-transform infrared spectroscopy spectrum which shows the example of a component analysis of a deposit. The flowchart which shows one structural example of the internal heat exchange type | mold distillation column used for the ethanol manufacturing apparatus of this invention.

  Next, embodiments of the present invention will be described in more detail with reference to the accompanying drawings.

  As shown in FIG. 1, the ethanol production apparatus 1 of this embodiment includes a pretreatment device 2, a saccharification treatment device 3, a fermentation treatment device 4, and a distillation tower system 5.

  The pretreatment device 2 includes a raw material supply device 21, an ammonia water supply device 22, a stirring tank 23, a storage tank 24, and a transfer conduit 25. The raw material supply device 21 supplies the raw material substrate to the stirring tank 23, and the ammonia water supply device 22 supplies ammonia water to the stirring tank 23. As the substrate, lignocellulosic biomass such as rice straw can be used.

  The agitation tank 23 agitates and mixes the substrate and the aqueous ammonia, and supplies the obtained substrate mixture to the storage tank 24. While the substrate mixture is stored for a predetermined time, the storage tank 24 dissociates lignin from the substrate without heating or swells the substrate to obtain a pre-saccharification product.

  The saccharification pretreatment product is taken out by a transfer conduit 25 connected to the bottom of the storage tank 24, and ammonia is separated by a solid-liquid separation device 26 provided in the middle of the transfer conduit 25. Is sent to the saccharification treatment apparatus 3. The solid-liquid separator 26 includes a recovery conduit 27 that recovers the separated ammonia as aqueous ammonia. The recovery conduit 27 is connected to the ammonia water supply device 22.

  The saccharification treatment apparatus 3 includes a saccharification treatment tank 31. A transfer conduit 25 is connected to the upper part of the saccharification treatment tank 31, and a saccharification enzyme supply device 32 is provided. A transfer conduit 33 for transferring the saccharified solution obtained in the saccharification treatment tank 31 to the fermentation treatment apparatus 4 is connected to the bottom of the saccharification treatment tank 31. In the middle of the transfer conduit 33, a solid-liquid separator 34 is provided to separate and remove the rice straw residue and the like contained in the saccharified solution.

  The fermentation treatment apparatus 4 includes a fermentation treatment tank 41, and a transfer conduit 33 is connected to the upper part of the fermentation treatment tank 41 and a fungus body supply apparatus 42 is provided. A transfer conduit 43 for transferring the fermentation solution obtained in the fermentation treatment tank 41 to the distillation tower system 5 is connected to the bottom of the fermentation treatment tank 41.

  In the middle of the transfer conduit 43, a separation device 44 for separating the inorganic compound contained in the fermentation solution, and a protein contained in the fermentation solution and the inorganic compound separated by the separation device 44 are separated from the fermentation solution. A filtering device 45 is provided. The separation device 44 includes a pH adjusting solution adding device 46 for adding a pH adjusting solution for adjusting the pH of the fermentation solution and an aggregation for aggregating the inorganic compound in order to separate the inorganic compound contained in the fermentation solution. And a flocculant addition device 47 for adding the agent. Examples of the flocculant include iron salts, aluminum salts, calcium salts, and the like.

  The filtration device 45 preferably separates the protein contained in the fermentation solution and the inorganic compound separated by the separation device 44 from the fermentation solution separately. For this reason, the filtration device 45 is provided with an inorganic compound filtration device (not shown) for separating the inorganic compound from the fermentation solution and a downstream side of the inorganic compound filtration device, and the protein is separated from the fermentation solution. And a protein filtration device (not shown).

  As the inorganic compound filtering device, a filter having an opening in the range of 75 to 500 μm, preferably 150 to 250 μm can be used. Further, as the protein filtration device, an ultrafiltration membrane having a molecular weight cut-off in the range of 1000 to 3500 or an ion exchange resin having a most frequent radius of 50 to 500 Å obtained by crosslinking acrylic or styrene with divinylbenzene is used. be able to.

  Moreover, you may make it provide only one of the pH adjustment liquid addition apparatus 46 and the flocculant addition apparatus 47. FIG.

  The distillation column system 5 includes a mash column 51, a rectifying column 52, and a dehydrator 53, and a transfer conduit 43 is connected to the upper portion of the mash column 51. The mash column 51 includes a transfer conduit 54 for transferring the column top liquid to the rectification column 52, and the rectification column 52 includes a transfer conduit 55 for transferring the column top liquid to the dehydrator 53, and the column bottom liquid mashing column 51. And a reflux conduit 56 for refluxing. The moromi tower 51 and the rectifying tower 52 are each provided with a heating device and a condenser (not shown). As the heating device, for example, devices for blowing steam into the bottoms of the mash column 51 and the rectifying column 52 can be used.

  Next, the operation of the ethanol production apparatus 1 will be described.

  In the ethanol production apparatus 1, first, rice straw as a substrate supplied from the raw material supply apparatus 21 and ammonia water supplied from the ammonia water supply apparatus 22 are stirred in the stirring tank 23 to obtain a substrate mixture. The obtained substrate mixture is supplied to a storage tank 24 connected directly below the stirring tank 23, and stored in the storage tank 24 for a predetermined time, thereby dissociating lignin from the rice straw without heating, Alternatively, a pre-saccharification product is obtained by swelling the rice straw.

  Since the pre-saccharification product contains aqueous ammonia, ammonia is separated by the solid-liquid separation device 26 provided in the middle of the transfer conduit 25 while being transferred to the saccharification treatment tank 31 by the transfer conduit 25. . As a result, the ammonia separation saccharification pretreatment product is transferred to the saccharification treatment tank 31. On the other hand, the ammonia separated by the solid-liquid separator 26 is recovered as ammonia water by the recovery conduit 27 and is returned to the ammonia water supply device 22.

  In the saccharification treatment tank 31, the saccharification enzyme supplied from the saccharification enzyme supply device 32 is mixed with the ammonia separation saccharification pre-treatment product supplied via the transfer conduit 25, and held for a predetermined time. As a result, a saccharified solution obtained by saccharifying cellulose, hemicellulose and the like contained in rice straw as the substrate is obtained.

  The saccharification solution is taken out by a transfer conduit 33 connected to the bottom of the saccharification treatment tank 31, and the rice straw residue and the like are separated and removed by a solid-liquid separation device 34 provided in the middle of the transfer conduit 33. Then, it is transferred to the fermentation treatment tank 41.

  In the fermentation treatment tank 41, the fermented bacteria or yeast supplied from the microbial cell supply apparatus 42 is mixed with the saccharified solution supplied via the transfer conduit 33 and held for a predetermined time. As a result, the sugar contained in the saccharified solution is ethanol-fermented with the fermenting bacteria or yeast, and a fermentation solution containing ethanol is obtained.

  The fermentation solution is taken out by the transfer conduit 43 connected to the bottom of the fermentation treatment tank 41 and transferred to the mash tower 51. If the fermentation solution is transferred without any treatment, the mash tower 51, the rectifying tower 52, the transfer. There is a concern that deposits may deposit on the conduits 54 and 55, the reflux conduit 56, and the like.

FIG. 2 shows a Fourier transform infrared spectroscopic spectrum of a deposit (attached deposit) that adheres and accumulates. From FIG. 2, it is recognized that the fermentation solution contains phosphate, silicate (1200 to 900 cm ⁻¹ , 700 to 500 cm ⁻¹ ), and protein (1625, 1537 cm ⁻¹ , amide bond). Therefore, the precipitate is considered to be a complex of phosphate, silicate and protein.

  The protein is an enzyme used for the saccharification, a fermenting bacterium used for the fermentation, or a component derived from a cell of the enzyme, the silicate is a component of rice straw itself, and the phosphate is the fermentation bacterium or enzyme. It is thought that it is a component used for culturing.

  Then, the said fermented solution is first supplied to the separation apparatus 44 provided in the middle of the transfer conduit | pipe 43, and inorganic substances, such as the said phosphate and a silicate, are removed. The removal of the inorganic substance in the separation device 44 is performed by adding a pH adjusting solution to the fermentation solution from the pH adjusting solution adding device 46 to adjust the pH of the fermentation solution, and thereby inorganic compounds such as phosphate and silicate. Can be carried out by precipitation. Further, the removal of the inorganic substance in the separation device 44 may be performed by adding a flocculant such as iron salt, aluminum salt, calcium salt or the like to the fermentation solution from the flocculant adding device 47 to agglomerate the inorganic compound. Good.

  At this stage, the inorganic compound separated by the separation device 44 still forms a precipitate or agglomerate and has not been removed from the fermentation solution. Therefore, the fermentation solution is then supplied to the filtration device 45, whereby the precipitate or aggregate of the inorganic compound and the protein are separated by filtration. The filtration device 45 is, for example, an inorganic compound filtration device composed of a filter having an opening in the range of 150 to 250 μm, and an ultrafiltration membrane having a molecular weight cut-off in the range of 1000 to 3500, or acrylic or styrene. It is possible to efficiently separate the precipitate or aggregate of the inorganic compound and the protein by providing a protein filtration device provided with an ion exchange resin having a maximum frequency radius of 50 to 500 mm cross-linked with divinylbenzene.

  The fermentation solution is supplied to the mash tower 51 after the precipitate or aggregate of the inorganic compound and the protein are separated and removed by the filtration device 45. In the moromi tower 51, the fermentation solution is distilled to obtain a first ethanol solution containing a higher concentration of ethanol than the fermentation solution as a tower top liquid. The first ethanol solution is taken out from the top of the mash column 51 and transferred to the rectification column 52 through the transfer conduit 54.

  In the rectifying column 52, the first ethanol solution is subjected to rectification, whereby a second ethanol solution containing ethanol having a higher concentration than the first ethanol solution is obtained as a column top liquid. The second ethanol solution is taken out from the top of the rectifying column 52, transferred to the dehydrating device 53 through the transfer conduit 55, and dehydrated. As a result, ethanol having a concentration of about 99.9% by weight is obtained as a product.

  That is, in the distillation column system 5, the mash column 51 functions as a recovery unit, and the rectification column 52 functions as a concentration unit. Note that the bottom liquid of the rectifying column 52 is refluxed to the mashing column 51 through the reflux conduit 56 and again used for distillation.

  In the ethanol production apparatus 1 of the present embodiment, the inorganic compound and the protein contained in the fermentation solution are removed on the upstream side of the distillation column system 5, so that deposits are deposited in the distillation column system 5. Can be prevented. Therefore, according to the ethanol production apparatus 1 of the present embodiment, the distillation tower system 5 can be smoothly and efficiently operated.

  The ethanol production apparatus 1 of the present embodiment includes a distillation tower system 5 including a mash tower 51, a rectification tower 52, and a dehydration apparatus 53, but the distillation tower system 5 is replaced with the mash tower 51 and the rectification tower 52. The internal heat exchange distillation column 6 shown in FIG. 3 may be provided.

  The internal heat exchange type distillation column 6 is a single distillation column having a structure in which a second distillation column 62 is disposed inside a first distillation column 61 and the inside and the outside of the second distillation column 62 are separated from each other. A distillation column 63 is provided. In the first distillation column 61, a transfer conduit 43 for transferring the fermentation solution from the fermentation treatment tank 41 is connected to the upper portion of the portion that is outside the second distillation column 62 as a fermentation solution supply means. At the same time, a gas supply conduit 64 for taking out the first gas obtained at the top of the column and supplying it to the second distillation column 62 is provided.

  The gas supply conduit 64 is provided with a dry vacuum pump 65 that depressurizes the inside of the first distillation column 61 in the middle, and is connected to the bottom of the second distillation column 62 on the downstream side of the dry vacuum pump 65. The first distillation column 61 includes a first extraction conduit 66 for extracting the column bottom liquid from the bottom of the portion that is outside the second distillation column 62. A heat exchanger 67 is provided in the middle of the first extraction conduit 66 to exchange heat between the fermentation solution supplied from the transfer conduit 43 and the bottom liquid and to preheat the fermentation solution.

  In addition, a steam pipe 68 that heats the first distillation column 61 by supplying steam directly into the first distillation column 61 is provided at the bottom of the first distillation column 61. In the internal heat exchange distillation column 6, the heat exchanger 67 and the steam pipe 68 constitute a heating means for heating the first distillation column 61.

  On the other hand, the top of the second distillation column 62 is provided with a second extraction conduit 69 for extracting the liquid at the top of the second distillation column 62, and ethanol as a product is extracted via the condenser 70. Is done. Further, the condenser 70 includes a reflux conduit 71 for refluxing the residual liquid into the second distillation column 62.

  According to the internal heat exchange distillation column 6, first, the fermentation solution supplied from the transfer conduit 43 to the first distillation column 61 is exchanged with the column bottom liquid of the first distillation column 61 by the heat exchanger 67. Then, it is preheated and further heated by the steam supplied from the steam pipe 68 to the first distillation column 61. As a result, the fermentation solution is distilled, and a first gas containing ethanol having a higher concentration than the fermentation solution is obtained at the top of the first distillation column 61. The first gas is supplied to the second distillation column 62 via the gas supply conduit 64. At this time, the inside of the first distillation column 61 is depressurized by the dry vacuum pump 65. Therefore, while the inside of the first distillation column 61 is in a reduced pressure state below atmospheric pressure, the inside of the second distillation column 62 is at atmospheric pressure, and the temperature in the second distillation column 62 is higher than that in the first distillation column 61. Becomes hotter.

  As a result, the first gas is further distilled in the second distillation column 62, and a second gas containing a higher concentration of ethanol is obtained at the top of the second distillation column 62. The second gas is taken out by the second take-out conduit 69, cooled by the condenser 70 and liquefied, so that an ethanol solution containing a higher concentration of ethanol than the fermentation solution can be obtained. The residual liquid in the condenser 70 is refluxed into the second distillation column 62 through the reflux conduit 71.

  Here, in the internal heat exchange type distillation column 6, the temperature in the second distillation column 62 is higher than the temperature in the first distillation column 61, so that heat is transferred through the side wall of the second distillation column 62. As a surface, the heat of the second distillation column 62 moves to the first distillation column 61. As a result of the heat transfer, the first distillation column 61 is further heated and the temperature of the second distillation column 62 is lowered, so that the work of heating and cooling can be reduced and the thermal energy required for distillation is reduced. can do.

  However, when the deposit adheres to and deposits on the side wall of the second distillation column 62 serving as a heat transfer surface, the precipitate acts as a heat insulating material, so that the heat transfer resistance increases. There is a concern that the heat transfer to the first distillation column 61 is hindered.

  However, according to the ethanol production apparatus 1 of the present embodiment, the protein and the inorganic compound are separated by the filtration device 45, so that deposits are prevented from being deposited on the side walls of the second distillation column 62. Thus, the internal heat exchange distillation column 6 can be smoothly operated. Therefore, the heat energy required for distillation can be further reduced as compared with the case where the mash column 51 and the rectifying column 52 are used.

  DESCRIPTION OF SYMBOLS 1 ... Ethanol production apparatus, 2 ... Pre-processing apparatus, 3 ... Saccharification processing apparatus, 4 ... Fermentation processing apparatus, 5 ... Distillation tower system, 44 ... Removal apparatus, 45 ... Filtration apparatus, 46 ... pH adjustment liquid addition apparatus, 47 ... Flocculant addition device.

Claims (7)

In an ethanol production apparatus comprising fermentation means for fermenting a saccharified solution of biomass, distillation means for distilling the fermentation solution obtained by the fermentation means, and transfer means for transferring the fermentation solution from the fermentation means to the distillation means ,
The transfer means includes separation means for separating the inorganic compound contained in the fermentation solution, and filtration for separating the protein contained in the fermentation solution and the inorganic compound separated by the separation means from the fermentation solution. And an ethanol production apparatus.   2. The ethanol production apparatus according to claim 1, wherein the separation unit includes an addition unit that adds a flocculant to the fermentation solution or an adjustment unit that adjusts the pH of the fermentation solution.   3. The ethanol production apparatus according to claim 1, wherein the filtering unit includes an inorganic compound filtering unit that separates the inorganic compound from the fermentation solution, and a downstream side of the inorganic compound filtering unit. An ethanol production apparatus comprising protein filtration means for filtering from a fermentation solution.   The ethanol production apparatus according to claim 3, wherein the inorganic compound filtering means is a filter having an opening in the range of 75 to 500 μm.   The ethanol production apparatus according to claim 3, wherein the protein filtering means is an ultrafiltration membrane having a molecular weight cut-off in the range of 1000 to 3500, or an ion having a maximum frequency radius of 50 to 500Å obtained by crosslinking acrylic or styrene with divinylbenzene. An ethanol production apparatus comprising an exchange resin.   The ethanol production apparatus according to any one of claims 1 to 5, wherein the distillation means is disposed in the first distillation column and the first distillation column so that the inside and the outside are isolated from each other. The second distillation column, the fermentation solution supply means for supplying the fermentation solution to the first distillation column, and the second distillation column by taking out the first gas obtained at the top of the first distillation column. A gas supply conduit for supplying to the gas, a pressure difference generating means provided in the middle of the gas supply conduit to make the pressure in the second distillation column higher than that in the first distillation column, and a bottom liquid of the first distillation column A first extraction conduit to be extracted; heating means for heating the first distillation column; a second extraction conduit for extracting a second gas obtained at the top of the second distillation column; and a second extraction conduit And a condenser for cooling and liquefying the second gas, and the side wall of the second distillation column is a heat transfer surface. Further comprising an internal heat exchanging type distillation column heat of the second distillation column is moved to the first distillation column Te ethanol production apparatus according to claim.   The ethanol production apparatus according to any one of claims 1 to 6, wherein the biomass is lignocellulosic biomass.

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