• 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 method for separating fructose from glucose in mixture containing both sugars is disclosed, wherein the separation is carried out with anion-exchange resins in bisulfite form in a 3-column-system which is fed continuously from bottom to top. The process permits the simultaneous collection of both glucose and fructose which are separated in have a minimum dilution, the chromatographic bed being wholly expolited, thus making the instant process economically interesting.
    公开号:SU1072818A3
    申请号:SU813251316
    申请日:1981-02-20
    公开日:1984-02-07
    发明作者:Панзолли Паоло；Барбаро Аурелио；Маймоне Адриано；Вальдизерри Марио
    申请人:Э.Н.И.Энте Национале Идрокарбури (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to a process for the separation of fructose anion exchange resins from glucose in glucose syrups that are isomerized with glucose isomerase, and in rastoured sugar thieves. A known method for separating a mixture of glucose and fructose in a solution involves passing an initial solution through an anion-exchange resin in the bisulfite form and elution of the glucose-containing fraction with water. a set of fractions enriched in each of the sugars separated from each other by elution with water. According to this method, the loading of the sugar mixture must be interrupted in order to fill the column with water for separation and from. boron fractions of glucose and fru | stozy. Upon completion of the elution of these fractions, the sugar solution / containing isomeric products is transferred back to the head to separate l. The disadvantages of this method are the high dilution of both sugars, separated on a column, and the low degree of separation of the isomers. The purpose of the invention is to increase the output and the separated. Sugars. The goal is achieved by the method of separation of a mixture of glucose and fructose in a solution that involves passing the initial solution through an anion exchange resin in a bisulfite form and eluting the glucose-containing fraction with water; the initial solution is passed downwards sequentially through two; the resin layer is removed; after passing the solution through the second resin layer. The drawing shows a flow chart of the process with successive stages of operation of three ion exchange columns. The method consists in tracing. Into column 1, a sugar mixture is fed from the bottom, which rises along the inside of the column and exits the last enriched fructose. Then the effluent is fed from the bottom to column 2. When equilibrium is established, column 3 is saturated with glucose and sugar mixture (stages a, b). During the discharge of the mixture from column 3, column 1 is still filled with the mixture to be separated, and from the top of column 2 only pure solution of fructose comes out. From column 3, the glucose retained by the resin is washed out with a solution, and a solution of pure glucose is obtained. At the stage (see drawing, the resin in column 1 is saturated with glucose until separation is possible, after which the saturated mixture is discharged, and the mixture containing the two isomers is loaded into column 2, from which the fructose enriched solution, which is sent In column 3. In step d, glucose elutes from column 1, column 2 is still loaded with a mixture of two isomers, and the fructose solution flows from the top of column 3.; In stage e, column 2 is not capable of participating more in separation and therefore Saha mix is discharged The effluent from column 3 is directed to column 1, which has already been regenerated. At the stage, glucose is eluted from column 2 and fructose is produced from column 1, while the mixture of two isomers is loaded again into column 3. Repeated In exactly the same way, the desired effect is obtained. As can be seen from the drawing, the stage is identical to stage A. Colon: we are loaded with strongly alkaline anion exchange resin {Damberlit 1RL-400, Duolite A 101 D), deposited using quaternary ammonium groups on divinylbenzene styrene polymer, crosslinked by 6-10%. The resin is activated with an aqueous solution of 5% metabisulphite. on three . The process temperature is 30-60 ° C, preferably 50 ° C. The length of the resin bed is 2-6 m, preferably 3-5 or 5 m. The concentration of the initial solution of the Sugar mixture is 30–70%, the flow rate is 0.2–1.5 per 1 .m section of the inside parts of the columns filled with the adsorbent. The desorption of glucose and the extraction of the sugar mixture from the saturated column and the subsequent filling of the active column is carried out with water at a flow rate equal to the speed, with which the discharge of the columns with the mixture for separation occurs. Example. A glass column with a diameter of 5 and a height of 100 cm was used, equipped with a water jacket for heating. The height of the resin substrates used to fill the three columns, for example, Amberlite 1PA-400, is in total 300 cm, and the volume lb. A Batson-Marlox pump is used to load the system with a sugar mixture and remove said mixture from carbon-containing clones containing saturated resins. The separation effect is checked at the exit of each column, in particular at the exit of the column producing the fruit, with the aid of a rim. rotation angle measurements (Parkin-Klmer-E 141 sex meter) and g refractive index measurement tools (Abbe refractometer); More thorough analyzes were carried out: by means of haeogram chromatography. ; Columns, thermostated. Fill with water dispersion. Activate the resin of the osteamystl 1 t with the help of 2 l of 5% -HOFo water solution of sodium bisulfite thief, skipping ef with: b / l. An excess of bisulfite, sodium is removed by interrupting a 18 L resin; water. The resin activated in this way allows for the expiration of vat: at least 200 production separation cycles. The pilot plant is loaded with a solution containing glucose and fructoROM in paeHfjx quantities} with a dry matter content of 60% (wei / vol.) With a flow rate and 0.83 l / H. After some time, a stream of glucose solution is obtained separately from the fructose stream from a pilot .us. : The fructose thus collected has a purity of 93%, and the solids content is 20-30% (w / v). The glucose flux, which is fed back to isomerization, has a purity of 73-85%, and the dry matter content is 2В32% (w / v). The mixture, returned to its original capacity, keeps both sugars in the Unchanged quantity and dry substances 57-59% (weight / volume). The yield of fructose relative to the mixture to be loaded is about 1-15% by weight. On the basis of 1 l of EMRI resin per day. yield of fructose (93% purity} equals about 2 kg. EXAMPLE 2. To determine the effect of the height of the Resin Pillar - separation quality, three columns are used, each with a diameter of 1.6 cm and ss height) Rec 120; 240 and 360 cm, filled with Amberlite 1PA-400, activated bisulfite. Resin support when using circulating temperature-controlled water in the outer jacket color. The resin bed is loaded with 100% invert sugar with a solids content of 50% (in EU / weight) at a speed of 30 cm / h. The analytical technique is used the same as in Example 1. The results show that for this flow rate the height of the resin layer increases with increasing product purity, but does not exceed 240 cm in two cases. Example 3. To determine the effect of the loading rate on separation, columns with a diameter of 1; 6 and a length of 360 cm, filled with Amberlite 1PA-40Q, accumulated with bisulfite, are kept at a temperature of 50 ° C. Cyclone is filled with a solution of invertyrr, sugar containing 50% iomers (weight / weight) at four speeds xJ15, 25–50, and 100 cm / h to addseTTiaeHHp. The degree of purity of the product decreases when the rate of cTit flow is more than optimal. ; P p and M: p 4. Getting fructose from glucose. Fructose is obtained directly from glucose using glucose isomermerdza and separated on a resin. The apparatus, designed for this purpose, is a jacketed shirt (7.8 mm in diameter and 9 o cm long), filled with 1 kg cellulose acetate sparks, including Arthrobacter sp. Cells, and a system of three full length jackets, with a length of 450 cm and a crossover of 26.5 liters, produced by Duolithm A 101 D - Diaprosin resin activated with bisulfite. Isomerization of glucose occurs continuously. When Filling, the colors for isomers are. with a solution of glucose with 50 - Brix and pH 7.0 and at a temperature of 20 ml. With a flow rate of 2 i; i / 4, the conversion of glucose to fructose occurs by 48%. The broken syrup is fed at the same speed into three separation columns in such a manner that all cycles of fructose from glucose are repeated. Tacre separation is carried out according to the method of Example 1, except that the column for the production of fructance is larger and allows the production of 6 kg of fructose per day with a purity of 93%. Selected glucose is mixed with additional glucose up to a concentration of 50 ° - Brix and the syrup formed is fed into the isomerization culture. Thus, when we offer, we offer the right sprinkler. There is a minimum dilution of sugars due to the excellent separation of the sugar mixture on resins washed with water, and a high yield of fruit. Toses with the use of an exclusively exchange resin and changing only the feeding method, which is now carried out from the bottom up with a counter current, using the resin filled krrlnk, unload it, while as the mixture is continuously passed, the discharge is performed when the column is saturated with glucose.
    S1072818
    Production of fructose 93% purity
    Table continuation
    Note: A R is a death; F -. Receiving fructose; recarnkurukhtsa mixture; G - glucose selection.
    权利要求:
    Claims (1)
    [1]
    METHOD FOR SEPARATING A GLUCOSE AND FRUCTOSE MIXTURE IN A SOLUTION, which involves passing the initial solution through an anion exchange resin in bisulfite form and eluting the glucose-containing fraction with water, with the exception that, in order to increase the yield of separated sugars, the initial solution pass from bottom to top sequentially through the dy of the resin layer, with the fruit. the toe-containing fraction is removed after passing the solution through the second resin layer.
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    同族专利:
    公开号 | 公开日
    YU41981A|1983-10-31|
    DD156430A5|1982-08-25|
    YU41969B|1988-04-30|
    IN154578B|1984-11-10|
    AU542267B2|1985-02-14|
    CS235513B2|1985-05-15|
    AU6730081A|1981-08-27|
    BR8100989A|1981-08-25|
    US4443267A|1984-04-17|
    AR228959A1|1983-05-13|
    ZW3581A1|1981-05-27|
    JPS56135000A|1981-10-22|
    HU194943B|1988-03-28|
    PL229785A1|1981-09-18|
    IT8020105D0|1980-02-22|
    ZA81879B|1982-03-31|
    GR74153B|1984-06-06|
    EG15668A|1986-06-30|
    IT1141370B|1986-10-01|
    PH16659A|1983-12-13|
    BG46308A3|1989-11-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US5795398A|1994-09-30|1998-08-18|Cultor Ltd.|Fractionation method of sucrose-containing solutions|
    US6224776B1|1996-05-24|2001-05-01|Cultor Corporation|Method for fractionating a solution|
    US6663780B2|1993-01-26|2003-12-16|Danisco Finland Oy|Method for the fractionation of molasses|US3131232A|1959-07-27|1964-04-28|Universal Oil Prod Co|Fluid-solid contacting process and flow control method therefor|
    JPS5420578B1|1970-12-09|1979-07-24|
    JPS5515259B2|1974-06-24|1980-04-22|
    JPS5118392A|1974-08-06|1976-02-13|Yutaka Seimitsu Kogyo Ltd| Hagurumakatakezuribanno kirikomiokurisochi |
    JPS547380B2|1975-12-17|1979-04-06|
    GB1585174A|1976-06-16|1981-02-25|Ici Ltd|Separation of sugars from mixtures|
    JPS5411275B2|1976-06-30|1979-05-14|
    JPS5625320B2|1976-08-24|1981-06-11|
    FI69248C|1976-12-21|1986-01-10|Mitsubishi Chem Ind|FOERFARANDE FOER REGLERING AV OPERATIONSPROCESSEN AV EN SIMULERAD ROERLIG BAEDD|
    JPS5376975A|1976-12-21|1978-07-07|Mitsubishi Chem Ind Ltd|Controlling method for pseudomoving bed|
    JPS6055162B2|1977-05-26|1985-12-04|Sanmatsu Kogyo Kk|
    JPS5420577A|1977-07-13|1979-02-16|Umetani Seisakushiyo Kk|Device of housing bicycle|
    US4319929A|1979-11-19|1982-03-16|Uop Inc.|Simulated countercurrent sorption process employing ion exchange resins with periodic backflushing|US4402832A|1982-08-12|1983-09-06|Uop Inc.|High efficiency continuous separation process|
    US5221478A|1988-02-05|1993-06-22|The Dow Chemical Company|Chromatographic separation using ion-exchange resins|
    US5176832A|1991-10-23|1993-01-05|The Dow Chemical Company|Chromatographic separation of sugars using porous gel resins|
    US5800624A|1996-10-22|1998-09-01|University Of Notre Dame|Membrane process for separating carbohydrates|
    US6296772B1|2000-03-23|2001-10-02|Corn Products International, Inc.|Split ion exchange system and method of operating|
    ITMI20051103A1|2005-06-13|2006-12-14|Cantine Foraci Srl|PROCEDURE AND PLANT FOR THE PRODUCTION OF GRAPE ZUCCHERINE PRODUCTS|
    AU2007202885B2|2007-06-21|2014-01-16|Naturalia Ingredients S.R.L.|Process and plant for producing sugar products from grapes|
    US7935189B2|2007-06-21|2011-05-03|Cantine Foraci S.R.L.|Process and plant for producing sugar products from grapes|
    US8414706B2|2007-06-21|2013-04-09|Cantine Foraci S.R.L.|Process and plant for producing sugar products from grapes|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    IT20105/80A|IT1141370B|1980-02-22|1980-02-22|METHOD AND EQUIPMENT FOR CONTINUOUS SEPARATION OF GLUCOSE FRUCTOSE FROM INVERTED SUGAR OR ISOMERIZED GLUCOSE SYRUP|
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