• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    In a method for the production of a volatile organic compound, such as ethanol, by continuous fermentation by yeast of a carbohydrate- containing substrate in a fermenter, fermentation liquor from the fermenter (F) (Fig. 1) is centrifugally separated (C) into a yeast concentrate flow (5) and a yeast-free flow (2), the yeast concentrate flow is recycled to the fermenter and the yeast-free flow is separated (RU) into a volatile organic compound- rich flow (9) and a residual flow, at least part of which is recycled (3) to the fermenter. The separation may be accomplished by distilling off the volatile organic compound or by extracting it with a solvent e.g. octanol in the case of ethanol. <IMAGE>
    公开号:SU1303034A3
    申请号:SU792719149
    申请日:1979-01-30
    公开日:1987-04-07
    发明作者:К.Дж.Энстрем Ларс
    申请人:Альфа Лаваль,Аб (Фирма)；
    IPC主号:
    专利说明:

    BACKGROUND OF THE INVENTION 1. Field of the Invention This invention relates to an alcohol industry. 1 and relates to a process for producing ethanol.
    The aim of the invention is to reduce the amount of wastewater and increase the speed of fermentation,
    Fig. 1 shows a flow chart according to the proposed method; Fig. 2 is the same; the fermentation is carried out in one stage with the extraction of ethanol from the fermented wort by the distillation method; Fig. 3 is the same; the I method is carried out in two successive stages; Fig. 4 is the same; ethanol is recovered by an extraction method.
    The technological scheme (Fig. 1) contains a fermentation tank 1, a centrifuge) separator 2, an apparatus 3 for you
    15
    heating and communicating with the extraction unit 18 by pipelines 22 and 23, the extraction unit 18 is provided with a pipe 24 for discharging stillage and through pipe 23 is connected to the pipe 25 for supplying the solvent, and the disillation unit 19 is connected to the pipe 26 for discharging ethanol.
    The proposed method according to the flowchart shown in FIG. 1 is carried out as follows.
    The fermentation tank 1 serves the fermented wort and yeast and conducts the continuous fermentation of the wort, during the fermentation process the fermented wort is diverted through line 5 to the centrifugal separator 2, where ethanol is not affected, mixer 4, the junction is -20 jerkly divided it into yeast and dehydration - pipelines 5–8 with the formation of a wort and periodically with the circulation circuit. It is centered through the device 11 sludge, the robust separator is connected via pipeline 9 to the mixer L.
    25
    The fermentation tank 1, the centrifugal separator 2, the apparatus 3 for the separation of ethanol are equipped with devices 10-12, respectively, for the withdrawal of gas, sludge and ethanol, and the pipeline 7 has a branch 13 for removing bards from the cycle. The mixer 4 communicates with the pipe 14 for feeding the wort into the fermentation tank 1,
    The technological scheme according to FIG. 2 contains the same structural elements, only the apparatus 3 for ethanol separation is a distillation cube 15 with a heat exchanger and additionally has a heat exchanger 16 and a refrigerator 17,
    The technological scheme according to FIG. 3 contains the same elements as those shown in FIG. 2, only it has a double set.
    The flow chart of FIG. 4 contains the same structural elements, only the ethanol separator is an extraction unit 18 in the form of a counter-extraction extraction column and a distillation unit 19 in the form of a fractionation column. The centrifugal separator 2 is connected by a pipe-running water 6 to an extraction unit 18, which is connected to the distillation unit 19 by a pipe 20, the distillation unit 19 has a device 21 for indirect
    thirty
    through the device 11, the yeast is returned via pipelines 9 and 8 through the mixer 4 to the fermentation tank. From the dehydrated wort, the ethanol is isolated in an apparatus 3 for ethanol recovery to produce bards. Ethanol according to fixture 12 is withdrawn into a collection (not shown), and the bard is divided into two streams, one of which is pasteurized at a temperature of from 60 to 100 ° C and returned to the fermentation tank, and the other is removed from the cycle. During fermentation, the NID broth35 is removed and the ethanol concentration is maintained at 4–5 wt.%. Extraction of ethanol is carried out by thermal or extraction method at atmospheric pressure. It can be sucked up by vacuum, but this process is not economical.
    The proposed method according to the flow chart of FIG. 2 is carried out as follows.
    Concentrated clarified wort through the pipeline 14 through the mixer 4 is fed into the fermentation tank 1,
    50 where it is continuously fermented, in which the stream of wort coming to the fermentation is mixed with the yeast suspension coming from the centrifugal separator 55 Pa - and partly with the bards coming from the distillation cube 13. In the centrifugal separator, 2 slurry is periodically separated and output from process through fixture 11,
    five
    heating and communicating with the extraction unit 18 by pipelines 22 and 23, the extraction unit 18 is provided with a pipe 24 for discharging stillage and through pipe 23 is connected to the pipe 25 for supplying the solvent, and the disillation unit 19 is connected to the pipe 26 for discharging ethanol.
    The proposed method according to the flowchart shown in FIG. 1 is carried out as follows.
    The fermentation tank 1 serves the fermented wort and yeast and conducts the continuous fermentation of the wort, during the fermentation process the fermented wort is withdrawn through line 5 to the centrifugal separator 2, where it is continuously separated into yeast and dehydrated wort and periodically withdrawn through the device 11 sludge
    through the device 11, the yeast is returned via pipelines 9 and 8 through the mixer 4 to the fermentation tank. From the dehydrated wort, the ethanol is isolated in an apparatus 3 for ethanol recovery to produce bards. Ethanol according to fixture 12 is withdrawn into a collection (not shown), and the bard is divided into two streams, one of which is pasteurized at a temperature of from 60 to 100 ° C and returned to the fermentation tank, and the other is removed from the cycle. During fermentation, the brozhoNIN gases are removed and the ethanol concentration is maintained at 4–5 wt.%. Extraction of ethanol is carried out by thermal or extraction method at atmospheric pressure. Vacuum can be dispensed, but this process is not economical.
    The proposed method according to the flow chart of FIG. 2 is carried out as follows.
    Concentrated clarified wort through the pipeline 14 through the mixer 4 is fed into the fermentation tank 1,
    where continuous fermentation is carried out, during which the stream of wort entering the fermentation is mixed with the yeast suspension coming from the centrifugal separator and partly with the bard stream coming from the distillation cube 13. In the centrifugal separator, 2 slurry is periodically separated and removed from the process through the device 11,
    Ethanol is isolated in the still tank 15 for heating which serves deaf or hot steam, in the case of using the latter the dilution is compensated for by increasing the concentration in the fermenting mash. The use of a hot steam avoids deposition on heat transfer surfaces. Ethanol passes through the pipeline and bard, gives almost all of the available heat to the stream entering the distillation cube through the heat exchanger 16.
    A small part of the bard stream is withdrawn from the circulation cycle through branch 13, the remaining stream is cooled in refrigerator 17 and fed through mixer 4 to the fermentation tank 1. During fermentation, fermentation gases are released from the fermentation tank 1 by fixture 10, the concentration of ethanol in the fermentation tank. Chan 1 is kept low at around 4% by weight while the wort is fermented almost on. 100%.
    In order to improve the efficiency of work, it is advisable to connect several fermentation tanks in series, as shown in FIG. 3. The method is carried out similarly to the technological scheme shown in FIG. 2, only the bard from distillation cube 15 is passed through heat exchanger 16 and cooler 17 and is divided partially into one stream fed to the fermentation tank 1 and partially to the stream that is fed to the fermentation tank 1. through mixer 4. Ethanol flow It comes from the distillation cube 15. The operating parameters are chosen so that the concentration of ethanol in the bard used in the fermentation process is about 4% by weight, and in the bard that is removed from the process is low.
    Alternatively, an extraction technique can be used to separate the ethanol. FIG. Figure 4 shows schematically such a process. The ethanol is separated off by introducing a stream of solvent through a cement unit 18, which is small. It polishes the volatile compound — ethanol and enters the distillation unit 19 through the pipeline, from which ethanol flows through the pipeline 26. The lower solvent flow from the distillation unit enters the extraction unit 18, pre-mixed with the solvent. Part
    flow, connected by a volatile organic compound, i.e. leaving the extraction unit 18, is discharged, and the rest is fed into the fermentation tank 1 through the mixer 4. It is advisable to heat the distillation unit 19 by indirect heating. Octanol is used as a solvent; ethanol from the solvent is fractionated. During fermentation, molasses is used with a concentration of 50-60 brix, while the ethanol content does not exceed 5% by.%., Its continuous removal from the fermented wort. Thermal and extraction separation of ethanol is carried out at atmospheric pressure, while the bard is divided into two streams, one of which is pasteurized at a temperature of from 60 to 100 ° C and returned to the fermentation stage.
    The concentration of carbohydrates in the fermented wort is maintained no higher than 5% by weight.
    Example 1. A fermentation tank with a stirrer containing 100 liters of clarified molasses with a density of 20 Brix is fed 10 kg of baker's yeast and is fermented, the temperature of the fermentation of the wort is maintained equal. 32 ° C, while the fermented sugar is converted to ethanol by 90% for 3 hours. By the end of the fermentation, ethanol is continuously removed from the wort in an amount that ensures its concentration in the wort is about 4% by weight. The fermented wort is separated by centrifugation into a slurry, a yeast concentrate, which is returned to the fermentation tank, and a dehydrated wort. From a depleted wort in a continuous stream, it is thermally distilled under. ethanol is atmospheric pressure, and a stream containing 25–35 wt.% solids is separated from the obtained bards and taken out of the cycle, and the rest is pasteurized at 60 ° C and returned to the fermentation stage.
    Example 2. The method is carried out analogously to example 1. Cane molasses is fermented with Schizosaccharomyces pombe yeast at atmospheric pressure, the pH of the medium is maintained at 4.5 and 32 ° C during the fermentation process, and the growth of yeast is controlled by air intake. The flow of the wort was fed to a t-distillation cube for distillation into
    the amount of 580 kg / h, the bard stream is 363 kg / h, the concentration of ethanol in it is 0%. 65 kg / h of steam containing 38% ethanol is withdrawn from the fermentation tank 26 kg / h of carbon dioxide . The following equilibrium conditions are maintained in the fermentation tank:
    5-10 cells / ml
    Yeast Air Ethanol
    Oh, 1 part per million 4.3%
    The total content of CB (15% of yeast yeast)
    Fermentable
    sugar 0.2%
    A continuous distillation stream of 152 kg / h with a solids content of 25% by weight was discharged.
    Example 3. The method is carried out analogously to examples 1 and 2, only the wheat wort is subjected to fermentation by the yeast Saccharomyces cerevisiae, the concentration of ethanol in the fermented wort is maintained at 5 wt.%. Extraction of ethanol was carried out by the extraction method at atmospheric pressure. The solvent used is octanol, which is separated from ethanol by fractionation. The bard obtained in this way is divided into two streams, one of which with a solids content of 35% by weight, is taken out of the cycle, and the other is pasteurized at 100 ° C and is returned to the fermentation stage.
    The proposed method allows for a greater amount of waste water due to the production of bards from high concentrations.
    J5
    20
    25
    by substances, i.e. 4-6 times more concentrated and increase the speed of digestion due to the high concentration of soluble non-enzymatic substances and maintaining a certain concentration of ethanol, which does not inhibit the process.
    权利要求:
    Claims (3)
    [1]
    1. A method of producing ethanol, which involves continuous fermentation of the wort in the presence of bards, its separation by centrifugation on the sludge and fermented wort with yeast, return of the yeast to the collection of wort and extraction of ethanol from the fermented wort to obtain bards, characterized in that, in order to reduce the amount wastewater and increase the speed of fermentation, when separating the fermented wort by centrifugation, the depleted wort is additionally separated from the yeast, and ethanol is released. from the latter in a continuous stream, the resulting bard is divided into two streams, one of which with a solids content of 25-30 to 35 wt.% is taken out of the cycle, and the other is pasteurized at BO-C, followed by its return to the stage fermentation.
    [2]
    2. Method POP.1, distinguished by 35 U and with the fact that the concentration
    Ethanol in the fermented wort is maintained at 4–5 wt.%.
    [3]
    3. The method according to claim 1, characterized by the fact that the extraction of ethanol is carried out thermally or
    extraction method at atmospheric pressure.
      .one
    Editor A.Vorovich
    Compiled by L. Pashinina
    Tehred L.Oleynik Proofreader M.Samborska
    Order 1228/58 Circulation 500, Subscription VNIIGSh State Committee of the USSR
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    Production and printing company, Uzhgorod, Projecto st., 4
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    引用文献:
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE7801133A|SE430171B|1978-01-31|1978-01-31|CONTINUOUS PROCEDURE FOR THE PRODUCTION OF ETHANOL IN A FERMENTOR ADDED TO A SUBSTRATE WITH HIGH CARBOHYDRATE CONCENTRATION, WHICH DISPOSES FERMENTATION LIQUID AFTER COMPOUNDING A FRENCH PREPARED FLUID ...|
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