• 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 process is disclosed for the regeneration of a sorbent, particularly an ion exchanger used in the recovery, isolation or production of sugars, wherein a regeneration solution is used which contains at least 20 meq/l of an alkali metal hydroxide or hydroxide of an alkaline earth metal having an atomic number of at least 20, and at least 1 % by weight of a monosaccharide or disaccharide.
    公开号:SU1228779A3
    申请号:SU803221449
    申请日:1980-12-25
    公开日:1986-04-30
    发明作者:Паннекет Вильхельмус
    申请人:Акцо Н.В. (Фирма)；
    IPC主号:
    专利说明:

    I
    The invention relates to chemical technology, specifically to the regeneration of sorbents from absorbed impurities, and can be used in the treatment of wastewater and sugar syrups,
    In the technology of sugar production from sugar beet, cationic and anion exchange resins are used to remove alkaline earth metal cations and maintain the required pH of the solution. In this case, the problem of their regeneration arises, which is desirable to be solved without creating a significant amount of salt waste with the presence of a high e (1) regenerative capacity.
    The aim of the invention is to increase the degree of regeneration.
    Example 1. Kationit May 1. C12 in calcium form is washed with diluted syrup, thus preparing it for regeneration. Then it is regenerated by passing 200 ml of a diluted syrup with lime removed, containing up to g / l (1 g-eq / l) of sodium hydroxide from the bottom up through the column for 1 hour at 60 ° C. Next, the cation exchanger in the column is washed for 30 min with 600 ml of diluted syrup with the removed lime substance at 60 ° C. The cation exchanger is then reused to remove calcium ions from the diluted syrup, characterized by a strength of 14.6 ° Bx, pH 8, 9 and calcium content of 4., 9 meq / l (137 mg CaO / l). The filtrate is collected in fractions and analyzed for calcium, mg CaO / l:
    Filtrate fractions, ml:
    5 4 4 3 2 5 8 20
    Thus, the cation exchanger according to this example absorbs 660 mg-SQV, calcium per liter of resin, and the degree of regeneration is 66%.
    The regenerate obtained in accordance with this example can be recycled by introducing carbonates into the formation stage.
    287792
    carbonate acid regenerate containing calcium saharath and unused sodium hydroxide; In the carbonation step (carbonate formation of acids under the action of carbonic acid), calcium sucrose is split into calcium carbonate and sucrose. Regeneration is carried out completely without water being added to the process during washing,
    This reduces its cost due to the absence of additional evaporation of water and prevents sugar loss.
    Example 2. Macro5 regeneration of porous phosphate-acid cation exchangers of type I Shas SYN102 AI-CZO Chemie, which is carried out according to measure 1,
    The diluted syrup treated 70 using a regenerating cation exchanger is characterized by a strength of 14.9 Bx, pH 8.5 and a calcium content of 5.4 mEq / l (150 mg CaO / l), Calcium 5 in fractions is , mg CaO / l:
    Filtrate fractions, ml;
    0-4
    4000 - 5
    5000 - 6
    000 000 000
    O 12 17
    Thus, the cation-exchange substance absorbs 156 mg-SQV calcium per liter of resin,
    PRI me R 3. The process is carried out with a milder flow of wastewater having a hardness of 125 mg CaO / l, using a cation exchanger similar to that shown in Example 1. Sewage water at a rate of 4000 ml / ton; filtered downwards through a column containing 200 ml of cation exchanger in Na-form. The filtration process is carried out until the hardness of the water leaving the column becomes equal to 10 mg CaO / l. Then regeneration is carried out by passing 200 ml of a solution containing 60 g (1.5 g-eq / l) of sodium hydroxide and 220 g of sucrose per liter, in upward direction through the column for 1 hour at 20 C. Then the column washed for 30 minutes with 600 ml of solution J containing 220 g of sugar-3rDi5 at 20 ° C and waste water to the absence of sucrose. Then the cleaning process is repeated. The filtrate is collected in fractions and hardness is determined in them, mg CaO / l:
    filtrate fractions, l:
    O 10 20 30 40
    10 20 30 40 42
    4 4 6 8 10
    Thus, the cation exchanger absorbs 895 mEq / l of hard ions.
    Example 4. Diluted syro-beet sugar, pre-purified from calcium, is subjected to demineralization using a strong acid cation exchanger in the H-form in accordance with example 1 and using a weakly basic macroporous styrene divinylbenzene anion exchanger in the form (1 mac A 2050). from top to bottom, ready-made decalcified diluted juice, having a strength of 14.5 Bx, pH 9.2, at a filtration rate of 1,200 ml / h and first through a column containing 200 ml of this cation-exchange resin, and ATEM through a column containing 200 ml of said anion exchange resin. Collect the filtrate until the pH of the resulting juice drops to 4.5. After that, both columns are washed from the Sugars with condensation water under a reverse flow of liquid.
    Then the cation exchanger is regenerated by passing from top to bottom for 30 min. 200 ml of a solution containing 120 g / l of sulfuric acid, followed by washing with condensation water to neutral wash water.
    The anion exchanger is regenerated by passing 400 g of the solution through it from top to bottom, which is obtained by adding calcium oxide to the molasses solution having a fortress of 19 ° B, until it contains 0.680 g-eq. CaO / l, at a filtration rate of 400 ml / h and 15 ° C. The regenerate contained in the column is washed with condensation water at 15 ° C and a filtration rate of 1200 ml / h until the strength of the effluent stream from the column drops to 0.5 ° Bx.
    Then both columns are used again to demineralize the diluted juice. After the strength of the juice has been brought up in both columns, all the filtrate is collected to
    2287794
    until the pH of the juice flowing from the last column drops to 4.5. The degree of purity of the original diluted juice is 89.49, the degree of purity of the filtrate is 98.63; based on the total weight of the filtrate, the amount of non-sugars is calculated, which is removed using the combined method and is 184 g / l of anion exchange resin.
    10 When using for the regeneration of the anion exchanger a solution of sugar syrup with a strength of 7 Bx with a calcium hydroxide content of 0.22 g-Sq./l in the amount of 1430 ml (filtration rate
    15 800 ml / h) regenerated 155 g of non-sugars per liter of anion exchange resin.
    Example 5. Regen - is performed. a set of Imac C 12 cation exchanger according to Example 1, but using 100 ml of decalcified diluted syrup containing 80 g of sodium hydroxide. per liter (2.0 g-eq / l).
    The calcium content in the selected fractions, obtained using the regenerated diluted syrup, is mg CaO / l of the diluted syrup:
    Filtrate fractions, ml:
    7 7 7 9 12 15 21
    In this case, a strong acidic cation-exchange resin absorbs 435 mg-csv. calcium per liter of resin, and the degree of regeneration is 43.5%.
    Example 6. The cation exchanger of example 1 is regenerated by using 200 ml of decalcified setration juice containing 1 g-eq./l potassium hydroxide as an eluent, with a strength of 13.8 Bx, pH 9 and a content of 3.7 mgeq.SaO / l. The calcium content in the fractions is mg CaO / l:
    Filtrate fractions, ml:
    55
    4 4 4 4 4 6 16
    S 1228779 6
    In this example, the cation exchanger absorbed in Example 1. In this example, 495 meq. calcium per liter regeneration rate of 27%.
    resin, the degree of regeneration of 49.5%. Thus, the regeneration of p and mep 7. Carry out the regeneration of sorbents by the described method
    the cation exchanger by the known method 5 allows to increase the degree of their regency (using non-alkaline donation by 2-2.5 times in comparison with
    sugar syrup solution) in a well known way.
    权利要求:
    Claims (1)
    [1]
    METHOD FOR REGENERATING SORBEN3 TOV by treating them with an aqueous solution of mono- and / or disaccharide, characterized in that, in order to increase the degree of regeneration, the treatment is carried out with a solution of mono / or disaccharide containing alkali or alkaline-earth metal hydroxide selected from the group consisting of from sodium, potassium and calcium, in an amount of 0.2-2.0 g-eq / L.
    >
    1 12
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    同族专利:
    公开号 | 公开日
    US4353992A|1982-10-12|
    PL228752A1|1981-09-04|
    JPS5697540A|1981-08-06|
    FI69765B|1985-12-31|
    TR21193A|1983-12-08|
    CS942780A2|1985-07-16|
    FI69765C|1986-05-26|
    IE50620B1|1986-05-28|
    BG49501A3|1991-11-15|
    MA19027A1|1981-07-01|
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    NL7909337A|1981-07-16|
    DZ258A1|2004-09-13|
    PT72243A|1981-01-01|
    DK157353C|1990-05-21|
    DK552380A|1981-06-29|
    DK157353B|1989-12-27|
    CS241479B2|1986-03-13|
    RO84534B|1984-08-30|
    HU183277B|1984-04-28|
    AT11112T|1985-01-15|
    YU42231B|1988-06-30|
    JPS6211615B2|1987-03-13|
    ES498184A0|1981-12-01|
    YU330280A|1983-10-31|
    FI804029L|1981-06-29|
    CA1150249A|1983-07-19|
    DE3069954D1|1985-02-21|
    IE802716L|1981-06-28|
    ES8201037A1|1981-12-01|
    DD155824A5|1982-07-07|
    PT72243B|1981-11-05|
    EP0032263A1|1981-07-22|
    GR72410B|1983-11-02|
    EP0032263B1|1985-01-09|
    RO84534A|1984-06-21|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    BE468493A|1945-10-27|
    US2482765A|1946-07-10|1949-09-27|Dorr Co|Sugar solution ion exchange|
    DE1104460B|1958-05-07|1961-04-06|Sandor Vajna Dr Ing|Process for the regeneration of anion exchangers used in the desalination of sugar solutions in an acid cycle|
    FR1404591A|1964-05-21|1965-07-02|Magyar Cukoripar Ki|Process for regenerating ion exchangers and for reducing the content of alkaline ions in juice from sugar factories, with a view to their use for the sweetening of diluted juices, by means of ion exchange|
    IT986260B|1972-06-29|1975-01-20|Pfeifer Und Langen|PROCEDURE AND PLANT FOR RECEIVING SUGAR FROM MOLASSA BY ION BREAKDOWN|
    US3791866A|1972-08-07|1974-02-12|Rohm & Haas|Recovery of waste brine regenerant|
    DE2362211C3|1973-12-14|1978-05-11|Sueddeutsche Zucker Ag, 6800 Mannheim|Process for processing molasses|US4533398A|1981-10-02|1985-08-06|Uop Inc.|Extraction of sucrose|
    US4741832A|1984-05-15|1988-05-03|The Trustees Of Columbia, University In The City Of New York|Purification apparatus and method employing a regenerable ligand|
    US5358915A|1993-02-12|1994-10-25|American Colloid Company|Process for regenerating spent acid-activated bentonite clays and smectite catalysts|
    IT1275974B1|1995-03-27|1997-10-24|Resindion S R L|TREATMENT PROCEDURE WITH A ION EXCHANGER RESIN OF A SUGAR SOLUTION DERIVED FROM BEET|
    PT101740A|1995-07-21|1996-04-30|Rar Refinarias Acucar Reunidas|PROCESS FOR REGENERATING IONIC PERFUME RESINS, USED FOR DECORATION OF ACUCAR, USING A SOLUTION OF SACRAROSE CONTAINING CALCIUM HYDROXIDE AND CALCIUM OR SODIUM CHLORIDE.|
    FR2753456B1|1996-09-18|1998-12-31|Generale Sucriere Sa|PROCESS FOR REGENERATION OF ION EXCHANGE RESINS IN THE DECALCIFICATION PROCESS OF SWEET JUICES|
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    CN110061210B|2019-04-15|2021-08-31|深圳市高能达电池有限公司|Preparation method and application of modified bagasse/sulfur composite material|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NL7909337A|NL7909337A|1979-12-28|1979-12-28|METHOD FOR THE REGENERATION OF SORBENTIA, IN PARTICULAR ION EXCHANGERS.|
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