• 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 for continuously separating, in liquid phase, fructose from a liquid feed mixture of sugars containing essentially fructose and glucose by contact with a solid sorbent of zeolite. The process utilizes a simulated countercurrent flow system wherein a liquid stream flows through serially and circularly interconnected desorption, rectification and sorption zones each zone being divided into a plurality of sections. In the zones water as desorbent is introduced into the desorption zone, the liquid feed mixture of sugars is introduced into the sorption zone, a desorption effluent is withdrawn from the desorption zone and a raffinate effluent is withdrawn from the sorption zone, and all of the points of introduction and withdrawal of the liquids are simultaneously shifted, one section at a time at predetermined intervals of time, in a downstream direction.
    公开号:SU1748648A3
    申请号:SU772514752
    申请日:1977-08-24
    公开日:1992-07-15
    发明作者:Одавара Хироюки；Оно Масадзи；Ямазаки Тору；Канаока Масазуми
    申请人:Торэй Индастриз, Инк. (Фирма)；
    IPC主号:
    专利说明:

    imitations of counterflow, in which the fluid flows are allowed to flow at a certain speed through desorption, rectification and sorption zones connected in series and closed with each other, having a certain number of columns and sections.
    Figure 1 shows an installation for implementing the method; Fig. 2 is a flow chart of the method.
    The installation contains a pipeline with 44 cranes and 11 vertical columns 1-11, interconnected in series. Each of the columns is divided into three zones: a desorption zone of 5 columns, a rectification zone of 2 columns, and a sorption zone of 4 columns. The internal diameter of each column is 25 mm, and its height is 1.5 m, the columns are filled with barium Y-type zeolite particles to a height of 1.35 m from the bottom, and the size of spherical particles is 0.5 mm. Copper particles 0.5 mm in size are also placed in each column, which fill the remaining free space to a height of 0.15 m from the upper level of the zeolite layer. In the entire column, there are 4.5 kg of zeolite particles. All tubes and taps have an internal diameter of 2 mm, and the distance between the column and the faucet that switches the points of injection and output of fluid flow into and out of the column is small enough to prevent contamination of fluid flow.
    The opening and closing of all taps is accomplished with software time management. The time required to open and close the taps is less than 1 s. The starting mixture used is an aqueous solution of 7% by weight of a sugar mixture containing 57.5% by weight of glucose and 42.5% by weight of fructose. The initial mixture is continuously fed at room temperature, through pipe 110 with a flow rate of 1.5 kg / h.
    As a desorbent, water is supplied at room temperature with a flow rate of 2.9 kg / h through pipe 120.
    Before filling two liquids, 4 cranes V2, V19, V29 and V36 are open, and the remaining 40 cranes are closed. After the start of filling, four cranes V6, V23, V33 and V40 are opened and at the same time the other 40 cranes are closed, due to which all points of input and output of fluid flows are shifted by one column. Similarly, all the points of input and output are simultaneously shifted at intervals of 6 minutes. The effluent raffinate is continuously withdrawn at a rate of 0.2 kg / h through a 1tO pipe. Exhaust stream contains sugar mixture.
    at a concentration of 45 wt.%, in water at a concentration of 55 wt.%. In the sugar mixture, fructose is present in a concentration of about 3%. The stream leaving the desorption zone,
    continuously discharged at a rate of 4.2 kg / h through pipe 130. In the discharge stream, the concentration of fructose and water is 1.0 and 99.0 wt.%, respectively. Almost no glucose is contained in the withdrawn stream. The circulation rate of the liquid stream in the rectification zone is about 8 5 kg / h.
    The yield of the excretion product - fructose is 90%, the purity of fructose in the products is 95%.
    Thus, the method allows the separation of mixtures of fructose and glucose on an industrial scale to produce fructose as a syrup in high yield.
    0 and high purity
    权利要求:
    Claims (1)
    [1]
    The invention of the method of extraction of fructose from a mixture of fructose and glucose in the form of an aqueous solution by the interaction of an aqueous solution
    5 mixtures of sugars with particles of solid sorbent, desorption of sugars with water and separation of fractions with a high content of fructose, characterized in that, in order to simplify the process, a method of continuous extraction in the liquid phase of fructose from a 7% aqueous solution of the fed sugar mixture is carried out containing 42.5 wt.% of fructose and 57.5 wt.% of glucose, selective sorption with 4.5 kg of solid sorbent particles in the form of barium zeolite V-type, having a size of 0.5 mm, using use of a simulated oncoming flow system It contains 11 columns, each of which has an internal diameter of 25 mm and a height of 1.5 m, where the liquid flows pass through three zones connected in series and in a circle, i.e. desorption zone containing 5 columns, zone
    5 rectification containing 2 columns and a sorption zone containing 4 columns, each zone being divided into a plurality of sections connected in series, each of which is filled with mass
    These solid particles of sorbent, and liquid streams flowing in three spaces, circulate continuously between the desorption zone and the sorption zone, while introducing the initial liquid mixture at room temperature.
    5 at a rate of 1.5 kg / h in the first section of the specified sorption zone; water is introduced as a desorbent at a flow rate of 2.9 kg / h in the first section of the specified desorption zone; the stream flowing from the desorption zone contains a sorbent and desorbent ,
    continuously withdrawn from the last section of the specified desorption zone at a rate of 4.2 kg / h, the raffinate stream is continuously withdrawn at a rate of 0.2 kg / h from such a point of the sorption zone that at least one section of the specified zone remains downstream , the circulation rate of the liquid stream in the distillation zone is 8.5
    kg / h, and all the points of entry and exit of these liquid streams in sections and from sections are simultaneously shifted by one section in a time interval b min in the direction of the flow flowing down, but the same order of sequence and the same spatial ratio is maintained between the specified points
    1
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1748648A3|1992-07-15|Method for separation of fructose from fructose-glucose mixture
    FI81268C|1990-10-10|KONTINUERLIGT SEPARATIONSFOERFARANDE BASERAT PAO SERIESTROEMNING.
    KR890000511B1|1989-03-20|High efficiency continuous separation process
    CN101128409B|2011-04-13|Product recovery from simulated-moving-bed adsorption
    SU686611A3|1979-09-15|Method of isolating normal paraffinic hydrocarbons from a mixture with isoparaffing and aromatic hydrocarbons
    SU984401A3|1982-12-23|Method of separating normal paraffin-base hydrocarbons from mihture containing isoparaffin hydrocarbons
    US8802913B2|2014-08-12|Reduction in flushing volume in an adsorptive separation system
    US3706812A|1972-12-19|Fluid-solid contacting apparatus
    US5156736A|1992-10-20|Simulated moving bed apparatus using a single sorbent bed for separating components from a fluid stream
    KR100741753B1|2007-07-23|Simulated moving bed adsorptive separation process using adsorption chambers in parallel and crystallizer and equipment used for the same
    US3455815A|1969-07-15|Sorption process
    KR100741752B1|2007-07-23|Simulated moving bed adsorptive separation process using single adsorption chamber for pre-treating feed and equipment used for the same
    GB1338752A|1973-11-28|Separation process of components of feed mixture utilizing solid sorbent
    US4184943A|1980-01-22|Fractionation in an adsorptive hydrocarbon separation process
    PL83276B1|1975-12-31|
    US3310486A|1967-03-21|Separation process for the recovery of high purity components of hydrocarbon mixtures
    RU2556668C1|2015-07-10|System and method of recovering products using simulated moving bed adsorption
    US2967148A|1961-01-03|Selective adsorption process and apparatus
    RU2564356C1|2015-09-27|System and method for extraction of products by absorption with imitated travelling ply
    KR100741751B1|2007-07-23|Simulated moving bed adsorptive separation process using two adsorption chambers in series and equipment used for the same
    US3979281A|1976-09-07|Continuous liquid extraction process with periodic flow of the denser stream
    RU2576306C1|2016-02-27|System and method for extraction of products with application of adsorption with pseudomoving layer
    RU2342971C2|2009-01-10|Method for extraction-chromatographic separation of components mixture
    US2468069A|1949-04-26|Liquid separation method and apparatus
    US9145343B2|2015-09-29|Process and apparatus for the simulated counter-current production ofpara-xylene, constituted by two adsorbers in series with a total number of 22 or fewer beds
    同族专利:
    公开号 | 公开日
    US4157267A|1979-06-05|
    JPS5326336A|1978-03-11|
    JPS5625320B2|1981-06-11|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3761533A|1970-07-23|1973-09-25|Toray Industries|Separation process of components of feed mixture utilizing solid sorbent|
    JPS5123360B2|1972-07-25|1976-07-16|
    JPS5515200B2|1975-02-21|1980-04-22|US4373025A|1976-05-27|1983-02-08|Uop Inc.|Process for the isomerization of glucose|
    US4358322A|1976-05-27|1982-11-09|Uop Inc.|Process for separating a ketose from an aldose by selective adsorption|
    JPS6055162B2|1977-05-26|1985-12-04|Sanmatsu Kogyo Kk|
    US4405455A|1978-11-02|1983-09-20|Mitsubishi Chemical Industries Limited|Adsorption separation apparatus|
    AU540231B2|1978-11-02|1984-11-08|Mitsubishi Kasei Corporation|Adsorption separation method and apparatus|
    US4226639A|1979-05-25|1980-10-07|Uop Inc.|Silica guard bed for adsorbent used in an aqueous system|
    US4293346A|1979-11-05|1981-10-06|Uop Inc.|Simulated countercurrent sorption process employing ion exchange resins with backflushing|
    US4319929A|1979-11-19|1982-03-16|Uop Inc.|Simulated countercurrent sorption process employing ion exchange resins with periodic backflushing|
    IT1141370B|1980-02-22|1986-10-01|Anic Spa|METHOD AND EQUIPMENT FOR CONTINUOUS SEPARATION OF GLUCOSE FRUCTOSE FROM INVERTED SUGAR OR ISOMERIZED GLUCOSE SYRUP|
    US4287001A|1980-02-25|1981-09-01|Uop Inc.|Esterified aluminosilicate adsorbent as for resolution of sugar components|
    US4472203A|1980-09-08|1984-09-18|Japan Organo Co., Ltd.|Method for the separation of glucose and fructose|
    US4422881A|1980-10-29|1983-12-27|Roquette Freres|Installation and process for the continuous separation of mixtures of sugars and/or of polyols by selective adsorption|
    US4533398A|1981-10-02|1985-08-06|Uop Inc.|Extraction of sucrose|
    US4412866A|1981-05-26|1983-11-01|The Amalgamated Sugar Company|Method and apparatus for the sorption and separation of dissolved constituents|
    EP0075611B1|1981-09-29|1986-01-02|Uop Inc.|Simulated countercurrent sorption process employing ion exchange resins with backflushing|
    JPS5858151A|1981-10-05|1983-04-06|Uop Inc|Approximate countercurrent sorption accompanied by backwashing using ion exchange resin|
    US4394178A|1981-12-10|1983-07-19|Union Carbide Corporation|Bulk lactulose/lactose separation by selective adsorption on zeolitic molecular sieves|
    US4421651A|1982-05-28|1983-12-20|Iowa State University Research Foundation, Inc.|Method of recovering adsorbed liquid compounds from molecular sieve columns|
    US4434051A|1982-06-07|1984-02-28|Uop Inc.|Multiple valve apparatus for simulated moving bed adsorption processes|
    US4478721A|1982-08-12|1984-10-23|Uop Inc.|High efficiency continuous separation process|
    US4404037A|1982-08-12|1983-09-13|Uop Inc.|Sucrose extraction from aqueous solutions featuring simulated moving bed|
    US4402832A|1982-08-12|1983-09-06|Uop Inc.|High efficiency continuous separation process|
    US4447329A|1983-06-13|1984-05-08|Uop Inc.|Continuous desalination process|
    US4572742A|1983-09-28|1986-02-25|The Graver Company|Precoat filter and method for neutralizing sugar syrups|
    US4498991A|1984-06-18|1985-02-12|Uop Inc.|Serial flow continuous separation process|
    JPH0677880B2|1985-09-02|1994-10-05|日立テクノエンジニアリング株式会社|Hot press|
    DE3667840D1|1986-02-06|1990-02-01|Uop Inc|AXIAL MULTI-WAY VALVE.|
    US5122275A|1986-05-08|1992-06-16|A. E. Staley Manufacturing Company|Simulated moving bed chromatographic separation|
    FI86416C|1988-06-09|1992-08-25|Suomen Sokeri Oy|Procedure for extracting betaine from molasses|
    US5198120A|1989-12-26|1993-03-30|Japan Organo Co., Ltd.|Process for fractional separation of multi-component fluid mixture|
    US5156736A|1991-05-07|1992-10-20|Schoenrock Karlheinz W R|Simulated moving bed apparatus using a single sorbent bed for separating components from a fluid stream|
    JP2962594B2|1991-06-12|1999-10-12|オルガノ株式会社|How to separate multiple components|
    FR2694019B1|1992-07-22|1994-10-14|Roquette Freres|Process for the production of mannitol.|
    FR2697023B1|1992-10-16|1994-12-30|Roquette Freres|Low-calorie glucose soluble polymer and process for the preparation of this polymer.|
    FI96225C|1993-01-26|1996-05-27|Cultor Oy|Method for fractionation of molasses|
    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|
    US5800624A|1996-10-22|1998-09-01|University Of Notre Dame|Membrane process for separating carbohydrates|
    JP4879392B2|2000-11-09|2012-02-22|日本錬水株式会社|Chromatographic separation method|
    AT412258B|2000-11-28|2004-12-27|Vogelbusch Gmbh|METHOD FOR SEPARATING MIXTURES|
    FI20010977A|2001-05-09|2002-11-10|Danisco Sweeteners Oy|Chromatographic separation method|
    US7141172B2|2001-09-27|2006-11-28|Purdue Research Foundation|Versatile simulated moving bed systems|
    US20060273013A1|2004-03-01|2006-12-07|Chin Nien-Hwa L|Versatile simulated moving bed systems|
    US7022229B1|2003-12-19|2006-04-04|Uop Llc|Adsorption separation system|
    US6979402B1|2003-12-19|2005-12-27|Uop Llc|Miniature actual moving bed assembly|
    US7332080B1|2004-11-16|2008-02-19|Uop Llc|Apparatus for salt free water softening|
    US7476616B2|2004-12-13|2009-01-13|Fsi International, Inc.|Reagent activator for electroless plating|
    US20090223881A1|2008-03-04|2009-09-10|Peter Villeneuve|Reverse Osmosis System with Dual Water Intake|
    FR2965819B1|2010-10-08|2013-02-22|Roquette Freres|PROCESS FOR PRODUCING HIGH-PURITY SORBITOL SYRUP FROM SUCROSE AND USES THEREOF|
    US8349175B1|2012-03-23|2013-01-08|Orochem Technologies, Inc.|Rotary valve apparatus for simulated moving bed separations|
    ES2606931T3|2013-07-30|2017-03-28|Clariant International Ltd|Procedure for reducing the saccharide content of juice concentrates|
    FR3077959B1|2018-02-22|2021-09-24|Roquette Freres|PROCESS FOR MANUFACTURING RESISTANT PEA DEXTRIN|
    FR3097855B1|2019-06-28|2021-07-23|Ifp Energies Now|Liquid phase separation of second generation sugars by adsorption on FAU type zeolite with Si / Al atomic ratio less than 1.5|
    FR3097863A1|2019-06-28|2021-01-01|IFP Energies Nouvelles|Liquid phase separation of 2G sugars by adsorption on an FAU type zeolite with an Si / Al atomic ratio greater than 1.5|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    JP10015176A|JPS5625320B2|1976-08-24|1976-08-24|LV931195A| LV5706A3|1977-08-24|1993-11-11|Fragmentation of fructose from fructose and gluten mixture|
    MD94-0020A| MD60C2|1976-08-24|1993-12-07|Process for the fruitose separation from the fruitose and glucose mixture|
    [返回顶部]