• 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:
    A flow of fermenting liquor from a fermentor is separated into a yeast concentrate flow, which is recirculated to the fermentor, and a yeast-free flow which is separated in a simple evaporator unit into a first ethanol-enriched vapor flow and a first liquid bottom flow. The first vapor flow is treated to produce the desired ethanol while a major part of the first liquid bottom flow is recirculated to the fermentor. A minor, residual part of the latter flow is fed to a stripping unit where it is separated into a second ethanol-enriched vapor flow and a second liquid bottom flow exhausted of ethanol.
    公开号:SU1463134A3
    申请号:SU802886102
    申请日:1980-02-26
    公开日:1989-02-28
    发明作者:Роланд Торссон Конни；Яан Виира Индрек
    申请人:Нобель Кематур Аб (Фирма)；
    IPC主号:
    专利说明:

    one
    This invention relates to the alcohol industry.
    The aim of the invention is to reduce energy costs and prevent scale formation.
    The wort is fermented, divided into a stream of yeast concentrate and fermented wort, the yeast concentrate is returned to the fermented wort, a vapor stream containing ethanol in the distillation, evaporation and desorption units is separated from the fermented wort, and the distillation stream is rectified in the distillation unit the column. The bard after the evaporation unit is divided into two parts, one of which is returned to the stage of fermentation of the wort, and the second part of the bard is subjected to separation in the desorption unit into an ethanol-rich vapor stream and vat residue. Part of the vapor stream is sent directly or indirectly to the distillation unit or mixed with a steam stream containing ethanol, obtained after its extraction from fermented wort, or it is used or the mixture is used to heat the rectification column. It is advisable after rectification formed
    four
    05
    Od
    with
    four
    cm.
    the fluid flow is recirculated;
    J. FIG. - 4 shows installation. to implement the method.
    The installation includes a fermenter 1, iieHTpo6eKHbrft separator 2, an evaporative unit 3, a desorbed unit 4 and a distillate unit 5, pipelines 6-16, a scrubber 17 and a heat exchanger 18.
    Example 1. According to FIG. 1, i: ycjio is fermented in a fermenter, in separator 2 it is divided into a stream of yeast concentrate and fermented: cond6. Yeast is recirculated through pipelines 6 and 7, and the fermented wort is directed through pipe 8 to the evaporator unit 3, where the 2GO is separated into a vapor stream containing ethanol and bard, which is transported through pipeline 9, - put into two parts, one of which is returned via pipeline 10 to the fermentation stage 1 to fermentor 1, and {circled through pipeline 1 1 is fed to desorption unit 4. The vapor stream, rich in ethanol, is fed through pipeline 12 to the distillation unit, where from the desorption unit 4 on. | Pipeline 13 also serves a steam stream. From the distillation unit, 5 is a stream of concentrated ethanol and a bottoms residue, consisting of: mostly from water and liberated more or less completely from ethanol. The cube residue can be used by vyshshaniem captured ethanol from a stream of carbon dioxide, as a result of fermentation, dp what it through pipeline 14 is fed into the scrubber 17, which through pipeline 15 from the fermenter 1 serves carbon dioxide. The resulting stream can be used to dilute the wort.
    The evaporation unit consists of a short column corresponding to one or more distillation cascades, and the desorption unit consists of a desorption column having a slightly larger number of distillation cascades, for example, made in the form of plates.
    Example 2. The method is carried out analogously to example 1, only according to FIG. 2, the desorption unit 4 consists of three evaporation cascades, arranged in series TciK, that the vat residue is presented sequentially and cascades, and the steam flow is returned from each subsequent stage to the previous one. The last stage is equipped with a heat exchanger 18 for indirectly supplying the energy required for desorption.
    Example 3. The method is carried out analogously to example 1, only
    according to FIG. 3, the evaporation unit 3 consists of a short column corresponding to one or more distillation cascades, and the desorption unit 4 consists of a desorption column with a slightly larger number of distillation cascades. The second stream of vapors, enriched with ethanol, is fed to the evaporation unit 3, from which the first stream of vapors leaves,
    Q is enriched with ethanol, and it is fed through conduit 12 to a condenser 19, consisting of one or more condensation cascades, from the top of which a smaller flow of volatile is emitted
    5 impurities, and from its bottom part through conduit 20 to the distillation-desorption column 21, equipped with a heater 22 and a refrigerator 23. From this column, a stream of eto NOL with a high ethanol content and a cubic residue with a low ethanol content are obtained. The energy for separation in the desorption unit 4 or in the evaporation unit 3 can be supplied through the heat exchanger 18 and the heater 24 or in the form of live steam in the evaporation unit 3.
    Example 4, Fng, 4 presents an example of a material balance, where T is the full flow; -F is a fermentable wort; NF is a solid dissolving unbased material, mainly salts, glycerin and other Organic impurities are not separately taken into account; DS is the sum of F + NF, t, e, dry BeujecTBO, DS for feed supplied is equal to 42.7 wt.%, Including added water, DS in the fermenter is equal to 25.8 wt.% (Yeast is not taken into account), they
    g is not included in the non-yeast stream fed to the evaporative unit. In the bard, DS is 27.0 wt.% And 35.1 wt.% In-waste, .22% bards are recycled to the fermenter with ethanol content of 2.8 wt.%. The energy for separation in the evaporation unit 3 and in the desorption unit 4 is served partly as indirect heating steam to the desorption unit 4 and partly
    five
    in the form of a pair of indirect heating or live steam from the outside into the evaporation unit 3.
    Possible to work with DS from 25 to 30 May.7,
    The proposed method allows to reduce energy consumption and stop scale formation in blocks.
    权利要求:
    Claims (2)
    [1]
    Claim 1. Method for producing ethanol, which includes fermenting the wort, dividing it into a stream of yeast concentrate and fermented wort, returning the yeast concentrate to the fermenting wort, separating the vapor stream containing ethanol in the distillation and evaporating units into the fermented wort to produce bards, rectification it in distillation (kx) cone and separation of bards into two
    parts, one of the first ones that are returned to the stage of fermentation of the wort, about 1 and 5, and so that, in order to reduce energy costs and prevent scale formation, the other part of the bards is subjected to separation in the stripping unit for vapor flow , enriched with ethanol, and still residue,
    In this case, part of the stream of vapors enriched in ethanol is sent to a distant block or mixed with a vapor stream containing ethanol obtained after its separation from fermented wort, or it is used or the mixture is used to heat the distillation column.
    [2]
    2. A method according to claim 1, characterized in that after rectifying a vapor stream containing ethanol, the resulting liquid stream is recycled to the evaporation unit.
    23
    PhieZ
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1463134A3|1989-02-28|Method of producing ethanol
    US6478965B1|2002-11-12|Recovery of fermentation salts from dilute aqueous solutions
    CN102665843B|2015-09-23|For the system and method that alcohol reclaims and stillage accessory substance is concentrated
    US4309254A|1982-01-05|Alcohol recovery process
    US7867365B2|2011-01-11|Ethanol distillation with distillers soluble solids recovery apparatus
    US10737195B2|2020-08-11|Chemical recovery by distillation of dilute aqueous solutions produced in advanced bio-fuels processes
    US9138678B2|2015-09-22|Membrane-augmented distillation with compression and condensation to separate solvents from water
    US20140018581A1|2014-01-16|Process to Remove Product Alcohol from a Fermentation by Vaporization under Vacuum
    JP2012531209A|2012-12-10|Recovery of higher alcohols from dilute aqueous solutions
    US4328074A|1982-05-04|Production of concentrated alcohol and distillery slop
    US20110108409A1|2011-05-12|Use of superheated steam dryers in an alcohol distillation plant
    US4305790A|1981-12-15|Multiple effect distillation method and apparatus
    CN104151135B|2016-05-18|The concentrated thermal coupling apparatus of the alcohol distillation of molasses raw material top grade and waste liquid and technique
    SU1303034A3|1987-04-07|Method for producing ethanol
    CN107418979A|2017-12-01|A kind of alcohol fuel energy-saving clean production method
    RU2007146073A|2009-06-27|METHOD AND INSTALLATION FOR PRODUCING MIXTURE OF ETHANOL AND WATER
    CN104262089B|2016-08-24|The method and device that the dehydration of a kind of bio-fuel is refined
    US2010929A|1935-08-13|Method of distilling alcohol-containing fermented liquors
    CN212356909U|2021-01-15|Fermented mash evaporation concentration and rectification protein powder co-production system
    CN110922302A|2020-03-27|Differential pressure distillation dehydration production process of fuel ethanol double-negative-pressure rough distillation tower
    CN110981696A|2020-04-10|Process and system for producing fuel ethanol by using double-coarse single-fine three-tower distillation low-concentration fermented mash
    US20020072100A1|2002-06-13|Method to separate ethanol from a fermentation broth
    CN211522068U|2020-09-18|System for producing fuel ethanol by using double-coarse single-fine three-tower distillation low-concentration fermented mash
    CN110468162B|2021-05-14|Production process and device for preparing fuel ethanol by one-time phase transition method
    RU2692914C1|2019-06-28|Method for combined production of rectified ethyl alcohol and distillate from fermented grain material
    同族专利:
    公开号 | 公开日
    DE3007138A1|1980-09-04|
    SE432441B|1984-04-02|
    GB2044799A|1980-10-22|
    DK158679B|1990-07-02|
    DE3007138C2|1988-05-05|
    AU5588880A|1980-09-04|
    JPS55120791A|1980-09-17|
    AU521932B2|1982-05-06|
    NL8001194A|1980-08-29|
    FI73737C|1987-11-09|
    CA1147678A|1983-06-07|
    ZA801082B|1981-03-25|
    PH18381A|1985-06-19|
    DK81480A|1980-08-28|
    FR2450277B1|1985-12-27|
    AR220444A1|1980-10-31|
    BR8001126A|1981-09-08|
    US4358536A|1982-11-09|
    US4522920A|1985-06-11|
    FI800561A|1980-08-28|
    DK158679C|1990-12-03|
    JPS597315B2|1984-02-17|
    FI73737B|1987-07-31|
    NZ192992A|1983-05-10|
    FR2450277A1|1980-09-26|
    IN152343B|1983-12-24|
    GB2044799B|1983-05-25|
    SE7901738L|1980-08-28|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US504074A|1893-08-29|dickerson |
    US1912010A|1929-08-02|1933-05-30|Disttilleries Des Deux Sevres|Direct rectifying process for the production of pure alcohol|
    US2010929A|1931-10-13|1935-08-13|Gustave T Reich|Method of distilling alcohol-containing fermented liquors|
    US2127138A|1934-04-25|1938-08-16|Gustave T Reich|Process for simultaneously evaporating and distilling liquids|
    US2152164A|1935-05-13|1939-03-28|Theodore O Wentworth|Distillation process|
    US2155134A|1935-12-05|1939-04-18|Deutsches Reich Reichsmonopolv|Fermentation process|
    US2372854A|1941-04-15|1945-04-03|Gustave T Reich|Yeast|
    US2358272A|1942-02-11|1944-09-12|Seagram & Sons Inc|Art of distilling spirituous liquors|
    US2434672A|1943-10-15|1948-01-20|Nat Distillers Prod Corp|Method of concentrating distillery still slop|
    US2440925A|1944-04-27|1948-05-04|Chemprotin Producs|Fermenting method|
    US2698826A|1951-02-13|1955-01-04|Merco Centrifugal Co|Alcohol manufacturing process|
    US2892757A|1955-11-14|1959-06-30|Puget Sound Pulp And Timber Co|Purification of alcohol|
    GB1109311A|1963-08-07|1968-04-10|Hiram Walker & Sons Scotland L|Improvements in or relating to the production of grain whisky|
    US3884770A|1970-10-02|1975-05-20|Klaus Misselhorn|Process for obtaining purified alcohol from fermented mash|
    SE430171B|1978-01-31|1983-10-24|Alfa Laval Ab|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 ...|
    SE432441B|1979-02-27|1984-04-02|Alfa Laval Ab|PROCEDURE FOR PREPARING ETHANOL BY CONTINUOUS SPRAYING OF A CARBOHYDRATE-SUBSTRATE, WHICH A DRINK WITH RELATIVE HIGH RATE OF SOLID SUBSTANCE RECOVERY|SE432441B|1979-02-27|1984-04-02|Alfa Laval Ab|PROCEDURE FOR PREPARING ETHANOL BY CONTINUOUS SPRAYING OF A CARBOHYDRATE-SUBSTRATE, WHICH A DRINK WITH RELATIVE HIGH RATE OF SOLID SUBSTANCE RECOVERY|
    SE432442B|1979-07-06|1984-04-02|Alfa Laval Ab|PROCEDURE FOR PREPARING ETHANOL BY CONTINUOUS SPRAYING OF A CARBOHYDRATE-SUBSTRATE, WHICH AN ETHANOLANRICATED FLUID IS SEPARATED UNDER VACUUM BEFORE DISTRIBUTING THE VETERINARY WINE|
    SE7908105L|1979-10-01|1981-04-02|Alfa Laval Ab|PROCEDURE FOR PREPARING ETHANOL BY CONTINUOUS RAISING OF POLYSACCHARIDE CONTAINING|
    US4582570A|1981-07-24|1986-04-15|Merix Corporation|Azeotropic dehydration distillation process|
    DE3143734A1|1981-11-04|1983-05-11|Hoechst Ag, 6230 Frankfurt|METHOD FOR THE CONTINUOUS RECTIFICATION OF AN ALCOHOL-CONTAINING LIQUID MIXTURE "|
    JPS6114796B2|1982-09-27|1986-04-21|Shinenerugii Sogo Kaihatsu Kiko|
    JPS5982081A|1982-10-29|1984-05-11|Sanwa Shoji Kk|Method and apparatus for treating fermentation liquid|
    AT388386B|1983-01-13|1989-06-12|Voest Alpine Ag|METHOD FOR OBTAINING AETHANOL FROM TRANSFERABLE SUGAR SOLUTIONS|
    DE3313530A1|1983-04-14|1984-10-18|Fried. Krupp Gmbh, 4300 Essen|METHOD FOR SEPARATING AETHANOL FROM A SOLUTION CONTAINING ATHANOL|
    US4617270A|1983-05-13|1986-10-14|Anderson Clyde G|Alcohol and distillers grain recovery process|
    SE449876B|1984-12-07|1987-05-25|Nobel Chematur Ab|PROCEDURE FOR PRODUCTING ETHANOL WITH AN ADDITIONAL CENTRIFUGAL SEPARATION STEP, PLACED EITHER BEFORE OR AFTER THE PRIMARY DISTILLATION STEP|
    AT384236B|1984-12-13|1987-10-12|Vogelbusch Gmbh|METHOD FOR CONTINUOUSLY WINNING FERMENTATION PRODUCTS|
    GB8601081D0|1986-01-17|1986-02-19|Distillers Co Carbon Dioxide|Removing water from ethanol|
    SE450897B|1986-01-31|1987-08-10|Nobel Chematur Ab|PROCEDURE FOR THE PREPARATION OF ETHANOL BY MELASSESHING|
    JPH0369274B2|1986-10-09|1991-10-31|Shinnenryoyu Kaihatsu Gijutsu Kenkyu Kumiai|
    WO1988002649A1|1986-10-10|1988-04-21|Erickson Donald C|Interexchanged cascade ethanol distillation|
    FR2608170B1|1986-12-12|1989-10-20|Speichim Equip Ind Chimiq|NEW PROCESS FOR THE CONTINUOUS FERMENTATION OF AN AQUEOUS MUST WITH A VIEW TO PRODUCING ETHANOL AND / OR YEAST BIOMASS|
    BR8702590A|1987-05-20|1988-12-13|Engenho Novo S A|CONTINUOUS PROCESS OF OPTIMIZED FERMENTATION FOR THE PRODUCTION OF ALCOHOL|
    US5091057A|1990-07-20|1992-02-25|Ethyl Corporation|Stripping process for water removal from alcohol|
    US5571703A|1993-12-23|1996-11-05|Controlled Environmental Systems Corporation|Municipal solid waste processing facility and commercial ethanol production process|
    US5407817A|1993-12-23|1995-04-18|Controlled Environmental Systems Corporation|Municipal solid waste processing facility and commercial ethanol production process|
    US7297236B1|2001-06-30|2007-11-20|Icm, Inc.|Ethanol distillation process|
    EP2534961A1|2003-03-10|2012-12-19|POET Research, Inc.|Method for producing ethanol using raw starch|
    US20050239181A1|2004-03-10|2005-10-27|Broin And Associates, Inc.|Continuous process for producing ethanol using raw starch|
    US20050233030A1|2004-03-10|2005-10-20|Broin And Associates, Inc.|Methods and systems for producing ethanol using raw starch and fractionation|
    DE10329941B3|2003-07-02|2004-10-14|Mostofizadeh, Chahpar, Prof.|Process for recovering highly concentrated ethanol solutions from low concentrated ethanol solutions for storing wind energy as electrical energy comprises evaporating a low concentrated ethanol solution and removing the vapor produced|
    US7810425B1|2004-08-12|2010-10-12|Michael Kessler|System for processing grains, carbohydrates, sugars, and oilseeds|
    WO2006119386A2|2005-05-02|2006-11-09|Broin And Associates, Inc.|Methods and systems for producing ethanol using raw starch and fractionation|
    FI118301B|2005-05-25|2007-09-28|St1 Biofuels Oy|A process for preparing an ethanol-water mixture|
    US7919289B2|2005-10-10|2011-04-05|Poet Research, Inc.|Methods and systems for producing ethanol using raw starch and selecting plant material|
    BRPI0715442B1|2006-07-21|2018-01-30|Xyleco, Inc.|METHOD FOR PRODUCING PRODUCTS FROM BIOMASS CELLULOSTIC OR LIGNOCELLULOSTIC MATERIAL|
    US7815741B2|2006-11-03|2010-10-19|Olson David A|Reactor pump for catalyzed hydrolytic splitting of cellulose|
    US7815876B2|2006-11-03|2010-10-19|Olson David A|Reactor pump for catalyzed hydrolytic splitting of cellulose|
    DE102007001614A1|2007-01-04|2008-07-10|Lrz Landhandels- Und Recycling-Zentrum Gmbh|Energy self-sufficient method for manufacturing bioethanol from lignocellulose, protein, starchy or sugary additional material, involves disintegrating additional material, and obtaining raw slurry from disintegrated additional material|
    FI20075288A0|2007-04-25|2007-04-25|St1 Biofuels Oy|Method and apparatus for preparing a mixture of ethanol and water|
    US20080299624A1|2007-06-01|2008-12-04|Edward Heslop|Continuous fermentation apparatus and method|
    BRPI0811326A2|2007-06-13|2014-12-30|Lesperance Bertrand|"SILAGE DISPOSAL RECOVERY, INSTALLATION, SYSTEM AND PRODUCT PROCESS"|
    DE102007033988A1|2007-07-19|2009-01-22|Acs Agrochemische Systeme Gmbh|Producing purified starch comprises grinding cereals containing starch in an air vortex mill to starch flour, separating bran from the flour and subsequently separating proteins from the flour|
    US7972825B2|2009-02-13|2011-07-05|Ene003, Llc|Integrated apparatus for ethanol production and extraction|
    US8450094B1|2009-03-03|2013-05-28|Poet Research, Inc.|System for management of yeast to facilitate the production of ethanol|
    MX2011009269A|2009-03-03|2011-09-26|Poet Res Inc|Fermentation of biomass for the production of ethanol.|
    US20100233771A1|2009-03-03|2010-09-16|Mcdonald William F|System for pre-treatment of biomass for the production of ethanol|
    US9068206B1|2009-03-03|2015-06-30|Poet Research, Inc.|System for treatment of biomass to facilitate the production of ethanol|
    FR2949348B1|2009-09-03|2012-11-02|Rhodia Operations|CONTINUOUS SEPARATION PROCESS|
    US9017523B2|2010-06-14|2015-04-28|Pinnacle Engineering, Inc.|Packed bed scrubber using a fusel oil solvent|
    US9238599B2|2011-12-07|2016-01-19|Exxonmobil Chemical Patents Inc.|Alkylaromatic process|
    WO2013096834A1|2011-12-23|2013-06-27|The Trustees Of Dartmouth College|System and method for enhancing biomass conversion using flow-through pretreatment|
    US10118107B1|2017-11-07|2018-11-06|Fluid Quip Process Technologies, Llc|Method and system for distilling alcohol in an alcohol production process|
    US10392590B1|2019-01-07|2019-08-27|Fluid Quip Process Technologies, Llc|Method and system for distilling alcohol in an alcohol production process|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE7901738A|SE432441B|1979-02-27|1979-02-27|PROCEDURE FOR PREPARING ETHANOL BY CONTINUOUS SPRAYING OF A CARBOHYDRATE-SUBSTRATE, WHICH A DRINK WITH RELATIVE HIGH RATE OF SOLID SUBSTANCE RECOVERY|
    [返回顶部]