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WO1991008815A1 - Procede a lit fluidise simule variable - Google Patents

Procede a lit fluidise simule variable Download PDF

Info

Publication number
WO1991008815A1
WO1991008815A1 PCT/US1990/007024 US9007024W WO9108815A1 WO 1991008815 A1 WO1991008815 A1 WO 1991008815A1 US 9007024 W US9007024 W US 9007024W WO 9108815 A1 WO9108815 A1 WO 9108815A1
Authority
WO
WIPO (PCT)
Prior art keywords
loop
control device
improvement according
flow rates
rates
Prior art date
Application number
PCT/US1990/007024
Other languages
English (en)
Inventor
Michael M. Kearney
Kathleen L. Hieb
Original Assignee
The Amalgamated Sugar Company
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by The Amalgamated Sugar Company filed Critical The Amalgamated Sugar Company
Publication of WO1991008815A1 publication Critical patent/WO1991008815A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
    • B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
    • B01D15/1814—Recycling of the fraction to be distributed
    • B01D15/1821—Simulated moving beds
    • B01D15/1828—Simulated moving beds characterised by process features
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
    • B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
    • B01D15/1814—Recycling of the fraction to be distributed
    • B01D15/1821—Simulated moving beds

Definitions

  • This invention relates to simulated moving bed chromatographic separators. It is particularly directed to a process control procedure which improves the separation characteristics of a simulated moving bed.
  • Simulated moving bed (SMB) technology is well developed for applications involving separating the components of a fluid.
  • Typical applications of simulated moving bed chromatography include the separation of fructose from fructose-glucose solutions and the separation of sucrose from sugar beet or sugar cane syrups.
  • Ion exchange resins are typically employed as sorbents for these applications. Solution components are differentially absorbed by the ion exchange resin so that a separation waveform develops within the simulated moving bed.
  • a typical simulated moving bed apparatus consists of several compartments (or individual columns) filled with solid sorbent.
  • a fluid conduit interconnects the upstream and downstream ends of the system to form a loop through which fluid is continuously recirculated. The constant flow of fluid through the loop is called "internal recirculation flow.”
  • a manifold system of pipes and valves is provided selectively to position an inlet for feed material, an inlet for desorbent, an outlet for a sorbed component and an outlet for a nonsorbed (or less sorbed) component. Each inlet and outlet communicates with a separate bed compartment. Feed material enters the system at a designated compartment and is moved through the sorbent by the continuous internal recirculation flow.
  • Sorbed component(s) which flow(s) at a relatively slow rate is removed from the sorbed component outlet.
  • Nonsorbed component(s) which flow(s) at a relatively fast rate is removed from the nonsorbed component outlet.
  • Desorbent is added at its inlet valve between the respective outlet valve positions of the sorbed and nonsorbed components.
  • step time the designated inlet and outlet valve positions are displaced downstream one position on the manifold to the next sorbent bed compartment, which may be a discrete section of a vessel, (such as a column) , or an individual such vessel, e.g., column.
  • the step time is chosen such that the designation of valves is properly synchronized with the internal recirculation flow. Under these conditions the system eventually reaches a steady state with specific product characteristics appearing at predetermined intervals in sequence at each valve position. This type of system simulates valves held in a single position while the solid sorbent moves at a constant and continuous rate around the recirculation loop producing constant quality product at each valve.
  • the simulated version more closely approaches the character of an actual moving bed system as the number of compartments and valve positions increase.
  • An important distinction between batch and simulated moving bed systems is that the internal recirculation flow is continuous in the simulated moving bed process. Except for very small adjust ⁇ ments to control internal pressure, the entering and exiting flow rates are continuous and constant, thereby approximating an actual moving bed system as closely as possible .
  • An equilibrated SMB system of the type disclosed by the aforementioned parent applications exhibits a steady state separation waveform along the path of the recircu- lation loop. This waveform moves along the path of the recirculation loop with valve switching synchronized to maintain the desired steady state.
  • the flow rates through the various individual sorbent compartments are controlled to modify the specific steady state waveform characteristics of the process. These modifications differentiate the process of this invention from conventional SMB processes.
  • the steady state waveform is modified by any combination of: (1) Operating the recirculation flow rates in a non-constant manner as a function of time within a given compartment or column during a step,
  • the resulting process may be regarded as a "Time Variable Simulated Moving Bed” process (TVSMB) .
  • TVSMB Time Variable Simulated Moving Bed
  • Controlling such a process requires special procedures. Highly responsive computer interaction monitoring and flow control devices are preferred. It is recognized, however, that the benefits of this invention could be realized to some extent through the use of manual control procedures.
  • the claimed process involves the recognition that during any given step in a SMB process, the optimum flow rates in the system are time variable.
  • B(t) may be either graphically or mathematically expressed and may be encoded in conventional fashion in a microprocessor or other mechanical, electrical, or electromechanical controller.
  • This controller can be interfaced with one or more variable speed pumps or comparable flow control devices to maintain the desired recirculation flow rate at each instant of elapsed time during a step.
  • the internal flow rates for the subsequent compartments may be derived from B(t) by adding subsequent inlet flow rates and subtracting subsequent outlet flow rates.
  • the circulation flow rate is monitored at a fixed location in the loop. Adjustments are made to the flow control devices in the loop, either continuously or periodically, in response to the flow rate detected at the monitor location. These adjustments are made to bring the actual flow rate detected into harmony with the circulation rate predicted or desired at the monitoring location at each instant of time elapsed during the specific step (of the sequence of steps constituting a process cycle) in progress.
  • FIG. 1 is a generalized schematic diagram configured to illustrate the first step of a typical process of the invention
  • FIG. 2 is a diagram similar to FIG. 1 but configured to illustrate a subsequent process step
  • FIG. 3 is a schematic diagram similar to those of FIGS. 1 and 2 configured appropriately for the first step of a specific embodiment of the invention
  • FIGS. 4 through 6 are graphical plots of flow rate functions descriptive of the embodiment illustrated by FIG. 3; and FIG. 7 is a schematic diagram of a pilot plant configured for step 1 of a specific embodiment of the invention.
  • FIG. 1 illustrates a process configuration consisting of N compartments, columns or separating sections.
  • C a separating section may consist of one or more compartments
  • Recirculation flow is maintained by one or more pumps P placed in the recirculation loop L.
  • Inlet valves I and outlet valves X are oriented on each pipe 11, 12, 13, 14, 15, 20 of the loop L interconnecting compartments C.
  • a basic recirculation flow rate function B(t) is specified for column Cl. That is, the flow rate R x (t) through column Cl during step 1 is a function of time specified as B(t) where "t" is the elapsed time, 0 to T, into step 1 (the first valving position) .
  • Required internal recirculation rates for all other columns in step 1 are determined by adding subsequent inlet functions and subtracting subsequent outlet functions.
  • FIG. 2 illustrates the system of FIG. 1 with the valve functions shifted as appropriate for step 2.
  • the recirculation flow rates for the respective columns are appropriately shifted.
  • the appropriate time variable rate which should be monitored by the flowmeter F during step 2 is R 2 (t) . It is apparent that in subsequent steps, 3 through N, the monitored time variable flow rate at flowmeter F should progress sequentially through each of the rates R 3 (t) through R H (t) as follows:
  • Valve positions are displaced downstream one position for each step, eventually returning to step 1 and recirculating setpoint R x (t) .
  • a control device D such as a central processing unit (CPU) is interfaced with the flowmeter F and the pump P in conventional fashion.
  • time variable circulation rates R N appropriate for each step N of the process are encoded, by means of software or otherwise, into or in operable association with the control device D so that an expected or predicted flow rate can be determined for each instant t of time elapsed during a time step interval T.
  • the flowmeter, or associated apparatus intermittently or continuously compares the actual flow rate detected at a time t with the predicted rate for that time.
  • the control device D reacts to that comparison by adjusting all or selected flow control devices, P, I, X, in the loop L to minimize any difference in the comparison.
  • Both analog or digital control devices are operable, but the logic capabilities of modern microprocessors are more than ample for this purpose. They are thus preferred from the standpoint of cost and versatility.
  • FIG. 3 Eight columns 31 through 38, respectively, are configured as in FIG. 3 for step 1 of a process. Three inlets and three outlets are functional in the positions shown. These valve functions are shifted downstream one position each successive step while maintaining the same relative positions with respect to each other.
  • the basic recirculation function is empirically determined to be as illustrated by FIG. 4.
  • the inlet I functions are as illustrated in FIG. 5.
  • the outlet X functions are as illustrated by FIG. 6.
  • recirculation rates at flowmeter F are controlled at the time variable rates R x (t) through R 8 (t), respectively, as the process is cycled through steps 1 through 8, respectively.
  • one or more outlet flow rates may need to be increased or decreased slightly during operation to maintain proper internal operating pressure.
  • a pilot plant system was configured with four columns 41, 42, 43, 44, each packed with an ion exchange resin.
  • FIG. 7 illustrates the configuration with inlet and outlet positions appropriate for step 1.
  • Variable frequency booster pumps PI, P2, P3, P4 provided in the recirculation loop between columns adjusted the recirculation flow rate at the flowmeter F in the recirculation loop between columns 44 and 41.
  • Flow functions were established as follows:
  • outlet 4 delivered high fructose extract and outlet 2 delivered a high glucose raffinate.
  • the flowmeter F and the pumps PI, P2, P3 and P4 were interfaced with a computer 50 in conventional fashion to maintain the specified flow rates.
  • the outlet flows were slightly increased or decreased from the functional setpoints as required to maintain proper internal pressure. Operating in this manner yielded a system production rate 22 percent greater than with the identical pilot plant configured for conventional simulated moving bed operation.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Analytical Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)

Abstract

On contrôle les débits à travers des compartiments individuels (31, 32, 33, 34, 35, 36, 37 et 38) du lit sorbant d'un lit fluidisé simulé suivant des fonctions à variables de temps afin de maintenir une forme d'onde d'état constant améliorée.
PCT/US1990/007024 1989-12-08 1990-11-30 Procede a lit fluidise simule variable WO1991008815A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US44767389A 1989-12-08 1989-12-08
US447,673 1989-12-08

Publications (1)

Publication Number Publication Date
WO1991008815A1 true WO1991008815A1 (fr) 1991-06-27

Family

ID=23777276

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1990/007024 WO1991008815A1 (fr) 1989-12-08 1990-11-30 Procede a lit fluidise simule variable

Country Status (3)

Country Link
AU (1) AU6908291A (fr)
WO (1) WO1991008815A1 (fr)
ZA (1) ZA909783B (fr)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5291259A (en) * 1992-11-12 1994-03-01 Eastman Kodak Company Image forming apparatus having toner cleaning device
US5293201A (en) * 1992-11-09 1994-03-08 Eastman Kodak Company Image forming apparatus in which toner is recycled between toner applying and cleaning stations
US5296905A (en) * 1992-11-12 1994-03-22 Eastman Kodak Company Cleaning device using magnetic particulate cleaning material
EP0688588A1 (fr) 1994-06-22 1995-12-27 Institut Francais Du Petrole Procédé de séparation par chromatographie en lit mobile simulé avec correction de volume mort par augmentation de débit
US5637225A (en) * 1993-05-10 1997-06-10 Xyrofin Oy Method for fractionating sulphite cooking liquor
FR2743002A1 (fr) * 1995-12-27 1997-07-04 Inst Francais Du Petrole Procede de regulation d'au moins un debit de fluide circulant dans une boucle de separation chromatographique en lit mobile simule
FR2754730A1 (fr) * 1996-10-18 1998-04-24 Novasep Sa Procede d'enrichissement d'isomeres optiques par lit mobile simule
FR2754731A1 (fr) * 1996-10-18 1998-04-24 Novasep Sa Perfectionnement aux procedes d'enrichissement d'isomeres optiques par lit mobile simule
US5795398A (en) * 1994-09-30 1998-08-18 Cultor Ltd. Fractionation method of sucrose-containing solutions
GB2326357A (en) * 1997-06-19 1998-12-23 Inst Francais Du Petrole Optimum operation of loops in a moving bed
EP1018561A1 (fr) * 1993-01-26 2000-07-12 Cultor Corporation Procédé de fractionnement de la mélasse
US6846657B2 (en) 1990-01-15 2005-01-25 Xyrofin Oy Process for the simultaneous production of xylitol and ethanol
US6875349B2 (en) 1996-05-24 2005-04-05 Cultor Corporation Method for fractionating a solution
US6896811B2 (en) 2001-05-09 2005-05-24 Danisco Sweeteners Oy Chromatographic separation method
US7109005B2 (en) 1990-01-15 2006-09-19 Danisco Sweeteners Oy Process for the simultaneous production of xylitol and ethanol

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3268605A (en) * 1961-11-06 1966-08-23 Universal Oil Prod Co Supervisory control system for a simulated moving bed separation process
US4182633A (en) * 1976-12-21 1980-01-08 Mitsubishi Chemical Industries Limited Process of the operation of a simulated moving bed
US4412866A (en) * 1981-05-26 1983-11-01 The Amalgamated Sugar Company Method and apparatus for the sorption and separation of dissolved constituents

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3268605A (en) * 1961-11-06 1966-08-23 Universal Oil Prod Co Supervisory control system for a simulated moving bed separation process
US4182633A (en) * 1976-12-21 1980-01-08 Mitsubishi Chemical Industries Limited Process of the operation of a simulated moving bed
US4412866A (en) * 1981-05-26 1983-11-01 The Amalgamated Sugar Company Method and apparatus for the sorption and separation of dissolved constituents

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7109005B2 (en) 1990-01-15 2006-09-19 Danisco Sweeteners Oy Process for the simultaneous production of xylitol and ethanol
US6846657B2 (en) 1990-01-15 2005-01-25 Xyrofin Oy Process for the simultaneous production of xylitol and ethanol
US7625728B2 (en) 1990-01-15 2009-12-01 Danisco Sweeteners Oy Process for the simultaneous production of xylitol and ethanol
US5293201A (en) * 1992-11-09 1994-03-08 Eastman Kodak Company Image forming apparatus in which toner is recycled between toner applying and cleaning stations
US5291259A (en) * 1992-11-12 1994-03-01 Eastman Kodak Company Image forming apparatus having toner cleaning device
US5296905A (en) * 1992-11-12 1994-03-22 Eastman Kodak Company Cleaning device using magnetic particulate cleaning material
EP1018561A1 (fr) * 1993-01-26 2000-07-12 Cultor Corporation Procédé de fractionnement de la mélasse
US5637225A (en) * 1993-05-10 1997-06-10 Xyrofin Oy Method for fractionating sulphite cooking liquor
FR2721527A1 (fr) * 1994-06-22 1995-12-29 Inst Francais Du Petrole Procédé de séparation par chromatographie en lit mobile simulé avec correction de volume mort par augmentation de débit.
US5582736A (en) * 1994-06-22 1996-12-10 Institut Francais Du Petrole Chromatographic simulated mobile bed separation process with dead volume correction using an increase in flow rate
EP0688588A1 (fr) 1994-06-22 1995-12-27 Institut Francais Du Petrole Procédé de séparation par chromatographie en lit mobile simulé avec correction de volume mort par augmentation de débit
US5795398A (en) * 1994-09-30 1998-08-18 Cultor Ltd. Fractionation method of sucrose-containing solutions
US5685992A (en) * 1995-12-27 1997-11-11 Institut Francais Du Petrole Process for regulating at least one fluid flow circulating in a simulated moving bed chromatographic separation loop
FR2743002A1 (fr) * 1995-12-27 1997-07-04 Inst Francais Du Petrole Procede de regulation d'au moins un debit de fluide circulant dans une boucle de separation chromatographique en lit mobile simule
US6875349B2 (en) 1996-05-24 2005-04-05 Cultor Corporation Method for fractionating a solution
FR2754730A1 (fr) * 1996-10-18 1998-04-24 Novasep Sa Procede d'enrichissement d'isomeres optiques par lit mobile simule
FR2754731A1 (fr) * 1996-10-18 1998-04-24 Novasep Sa Perfectionnement aux procedes d'enrichissement d'isomeres optiques par lit mobile simule
WO1999047228A1 (fr) * 1997-03-04 1999-09-23 Novasep S.A. Perfectionnement au procede d'enrichissement d'isomeres optiques par lit mobile simule
US6409923B1 (en) 1997-03-04 2002-06-25 Novasep S.A. Method for enriching optical isomers by means of simulated mobile bed
GB2326357A (en) * 1997-06-19 1998-12-23 Inst Francais Du Petrole Optimum operation of loops in a moving bed
US6471870B2 (en) 1997-06-19 2002-10-29 Novasep Method intended to optimize the operation of a system for separating the constituents of a mixture
GB2326357B (en) * 1997-06-19 2001-01-10 Inst Francais Du Petrole Method of optimising operation of a system for separating constituents in a mixture
FR2764822A1 (fr) * 1997-06-19 1998-12-24 Novasep Methode pour optimiser le fonctionnement d'un systeme de separation des constituants d'un melange
US6896811B2 (en) 2001-05-09 2005-05-24 Danisco Sweeteners Oy Chromatographic separation method

Also Published As

Publication number Publication date
AU6908291A (en) 1991-07-18
ZA909783B (en) 1991-10-30

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