• 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:
    Procédé de production de dextrose cristallisé monohydrate dans lequel la masse M soumise à la cristallisation parcourt de haut en bas, en continu et sous malaxage, une enceinte 1 à l'intérieur de laquelle elle est soumise à un gradient de température globalement décroissant de haut en bas, la masse cristallisée étant récupérée en continu en bas de l'enceinte, des moyens étant prévus pour prélever à un niveau intermédiaire 8 une fraction de la masse M et à la recycler à un niveau 9 situé au voisinage de l'extrémité supérieure de l'enceinte.
    公开号:SU1452485A3
    申请号:SU843817591
    申请日:1984-11-16
    公开日:1989-01-15
    发明作者:Бодель Жильбер；Дюфло Пьеррик；Валентэн Бернар；Юшетт Мишель
    申请人:Рокетт Фрэр (Фирма)；
    IPC主号:
    专利说明:

    4ib
    sl to
    4a
    00 cl

    cm
    The invention relates to the technology of producing -dextrose monohydrate
    The purpose of the invention is to increase the output of glucose.
    The drawing shows a flow chart of the method.
    Glucose syrups obtained by acid hydrolysis and enzymatic hydrolysis of starch with a dry matter content of about 55-85% by weight are used as starting material, and glucose is at least 60% and preferably above 90% by weight, calculated on dry matter syrup
    This concentrated syrup is fed through conduit I to a vertical or inclined crystallizer 2, in which it is moved using blades 3 mounted on shaft 4, uninterruptedly from top to bottom. Inside: the crystallizer I, cooling elements 5 are installed to provide the required temperature in the crystallization zone.
    ; The temperature of the syrup is adjusted or; the crystallization zone is maintained at the moment of its introduction in the range of 30-: 70 s, preferably at 35-55 ° C, and in practice it is close to 40-50 ° C. : The temperature gradient, which is established in the crystallization zone in the I mass undergoing crystallization, I corresponds to a decrease of 0.5–5 C, preferably 1–4–4 C per linear meter of the I crystallization zone and such that I at the output from the specified zone in the point located near the bottom of its end, the mass subjected to crystallization, which includes the syrup, the initial crystals and crystals formed in the crystallization process, was brought to a temperature in the range of 15-40 C, preferably 20-30 o.
    As the mass undergoing crystallization approaches the lower end of the crystallization zone, it is enriched with monohydrate dextrose crystals, and this mass at the exit of the zone forms a crumbly mass.
    At the intermediate level of the crystallization zone, at least 1/6 of its entire length from its ends, its fraction is subjected to crystallization of the mass, which
    0
    five
    0
    five
    0
    five
    0
    five
    0
    five
    recirculated through pipeline 6 to the beginning of the crystallization zone.
    The recycled fraction is 10-40% by volume, preferably 25-35% of the volume of glucose syrup charged to the crystallization zone.
    The amount of glucose syrup loaded is chosen so that the average residence time, statistical or theoretical, of the mass subjected to crystallization in the crystallization zone is 10-40 hours, preferably 20-30 hours. The preferred loading amount depends on the heat exchange properties of the agents constituting the crystallization zone by means of which a decreasing temperature gradient is established within said zone in a mass subjected to crystallization.
    The intermediate level at which the selection of the crystallized fraction intended for recirculation is carried out is at least a quarter of its entire length from the ends of the crystallization zone and is of the order of at least two fifths of the entire length of this zone.
    The viscosity of the mass that is subjected to crystallization increases as the fraction of the polyhydrate crystals increases, as is the case of dextrose, i.e. in the direction of lowering the temperature, the reason is that the crystallization zone is equipped with a means for transporting recycled mass (not shown)
    On the other hand, the blades 3 must be installed in such a way that the dead zones are eliminated and that the heat exchange between the mass to be crystallized and the cooling elements 5 is of a generally turbulent type.
    An otfel, including monohydrate dextrose crystals with a particle size spectrum that differs in an insignificant proportion of small and large crystals, and therefore 5 large proportions of intermediate-sized crystals, is removed from the crystallization zone through conduit 7.
    Example 1. A device is used that includes a cylindrical chamber with a usable volume of 48 m at a height of 8 m. In this chamber, with a flow rate of 1.8 m E, WATER glucose syrup 6 with a dry matter content of 74% and comprising 94 wt.% Dry matter of glucose, the remaining 6% being polysaccharides. The temperature of the syrup at the entrance to the chamber is about 50 ° C. At the same time, the fraction of the crystal mass taken at the middle level of the chamber is recycled at a rate of 0.5.
    The duration of the average passage inside the chamber of this fraction of mass, subjected to crystallization, is about 25 hours.
    The masonry mass, recoverable at the bottom of the mold, is at a temperature close to 25 ° C, with a generally decreasing temperature gradient from top to bottom corresponding to about 3.2 C per meter.
    The content of hydrols in glucose, extracted after the separation of monohydrate dextrose crystals, is 84% calculated on dry substances; the rest up to 100% is formed by polysaccharides.
    The yield of crystals is determined by the formula
    A - H
    g
    100 - N
    where a is the glucose content in the loaded syrup,
    H is the hydrol content of 62.5%.
    On day 1, 26.6 tons of monohydrate dextrose are obtained, which corresponds to a productivity of 0.55 tons per day per m of chamber.
    This result is close to that which is obtained during the crystallization of the same glucose syrup in a horizontal reactor, whose capacity is set to 0.3 tons per m of chamber per day.
    The process proceeds without disturbing the parameters of the crystallization process.
    The crystals obtained after centrifugation and klerovani possess excellent physical and chemical properties.
    These crystals have a purity of 99.5%. The height of the layer of their runoff is good and their particle size distribution is the following μ,%:
    crystals size
    more than 100
    crystals size
    60-80
    38 16
    five
    0
    five
    crystals size 80-10018
    Example 2. Analogously to example 1, an installation is used comprising a cylindrical chamber with a usable volume of 48 m and a height of 8 m. 1.8 glucose syrup with a dry matter content of 74%, in which the glucose is 94 wt.%, Is introduced into this chamber. and the remaining 6% are polysaccharides. The temperature of the syrup at the inlet of the chamber is about 50 ° C.
    As in Example 1, a fraction of the crystallizing mass selected at approximately the middle level of the chamber is recycled at a rate of 0.5.
    The duration of the average passage inside the chamber of a given fraction, the crystallization of the mass, is about 25 hours.
    The massecuite discharged from the bottom of the mold has a temperature of about, while the temperature gradient, generally decreasing from top to bottom, corresponds to approximately 3.2 ° C per meter.
    The glucose content of the effluents collected after the separation of monohydrate dextrose crystals is 1.84%, and the rest up to 100% is polysaccharides. In addition, the crystallization coefficient is the same as the coefficient determined in Example 1.
    After a certain number of hours of operation, and in contrast to the conditions specified in Example 1, the recirculated fraction is no longer selected at the intermediate level, but rather at the point of the chamber located on the last sixth part of its total height. In this case, a rapid change in the crystallization parameters occurs, which after several days expresses itself in a poor separation in centrifuges and makes it necessary to stop the installation and remove the mass contained in it. This adhesion of the work is the result of the granulometry of the resulting product
    too thin and too heterogeneous to such an extent that selection becomes impossible.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    I. Method for continuous production of dextrose monohydrate, which involves the introduction of a syrup containing at least 55% solids and 60% glucose into the upper part of a vertical or inclined crystallizer, the introduction of seed crystals into the syrup, moving the crystal from top to bottom of the tank while reducing its temperature and mixing and withdrawal of the finished massecuite from the crystallization zone, o tl and h a J3 3
    so that, in order to increase the yield of glucose, crystals are used as seeds) in an amount of 10-40% of the volume of the initial syrup, taken from crystallization aids located at least 1/6 of the total length of its beginning and end, and recycle this mass at the beginning of the crystallization zone.
    2, Method Pop, 1, differs by the fact that the amount of crystal mass taken is 25–35% of the volume of the initial syrup.
    .m
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    同族专利:
    公开号 | 公开日
    DE3468905D1|1988-02-25|
    KR920006867B1|1992-08-21|
    ES8600405A1|1985-10-16|
    FI844490L|1985-05-18|
    EP0147269A3|1986-04-02|
    ES537579A0|1985-10-16|
    EP0147269B1|1988-01-20|
    JPS60123493A|1985-07-02|
    KR850003737A|1985-06-26|
    AU564900B2|1987-08-27|
    EP0147269A2|1985-07-03|
    FI844490A0|1984-11-15|
    FR2555201B1|1986-10-31|
    FI78927C|1989-10-10|
    AU3563284A|1985-05-23|
    CA1242712A|1988-10-04|
    AT32103T|1988-02-15|
    JPH052319B2|1993-01-12|
    FR2555201A1|1985-05-24|
    US4620880A|1986-11-04|
    FI78927B|1989-06-30|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US1021173A|1912-01-09|1912-03-26|Hermann Wiese|Process of refining sugar.|
    US2823242A|1953-09-08|1958-02-11|Phillips Petroleum Co|Process and apparatus for crystal purification and separation|
    US2800411A|1954-03-31|1957-07-23|Phillips Petroleum Co|Crystal purification apparatus and process|
    FR1154584A|1955-07-02|1958-04-11|Buckau Wolf Maschf R|Continuous crystallization process of concentrated glucose|
    FR1295543A|1961-04-28|1962-06-08|Aquitaine Petrole|Method and apparatus for crystallization|
    DE1642536A1|1966-10-28|1971-05-06|Struthers Scient And Internat|Process for the continuous crystallization of dextrose|
    GB1210512A|1967-03-07|1970-10-28|Tate & Lyle Ltd|Method of, and apparatus for, continuously producing crystals from a solution|
    BE727378A|1967-07-13|1969-07-24|
    US3617382A|1968-07-17|1971-11-02|Christos B Natsis|Mixing apparatus as used in mass and heat transfer processes|
    DK147287C|1977-01-13|1984-11-05|Danske Sukkerfab|COOLER FOR CRYSTAL BLENDS AND CRYSTALLIZING LIQUID IN THE SUGAR PRODUCTION AND RELATED PRODUCTS|
    FR2493869B1|1980-11-10|1983-12-23|Fives Cail Babcock|
    US4357172A|1980-12-17|1982-11-02|Cpc International Inc.|Process for continuous crystallization of alpha monohydrate dextrose utilizing high agitation|FR2582016B1|1985-05-15|1987-09-18|Roquette Freres|PROCESS AND PLANT FOR THE PRODUCTION OF ANHYDROUS CRYSTALLIZED FRUCTOSE|
    FR2582015B1|1985-05-15|1987-09-18|Roquette Freres|PROCESS AND PLANT FOR THE PREPARATION OF ANHYDROUS CRYSTALLIZED DEXTROSE|
    DE3541576A1|1985-11-25|1987-05-27|Krupp Gmbh|METHOD FOR DEXTROSE MONOHYDRATE CRYSTALLIZATION|
    IT1313586B1|1999-07-30|2002-09-09|Vomm Chemipharma Srl|METHOD OF CRYSTALLIZATION OF SORBITOL AND CRYSTALLIZED SORBITOL WHAT IS OBTAINED.|
    CN101381384B|2008-09-11|2012-09-26|西王集团有限公司|Crystallization method of monohydrate glucose|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR8318318A|FR2555201B1|1983-11-17|1983-11-17|PROCESS AND PLANT FOR PRODUCING CRYSTALLIZED MONOHYDRATE DEXTROSE|
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