Abstract
In this chapter, the use of ion exchange resins in continuous sugar process industry is reviewed. A particular focus is given to chromatographic methods and, in particular, to continuous annular chromatography and simulated moving-bed (SMB) apparatus. The use of ion exchange resins for the separation of a fructose and glucose mixture (by means of an SMB unit) and the separation into pure components of a ternary mixture of sugars (by means of a Pseudo-SMB technique) is detailed. The use of ion exchange resins in integrated reactors (separation in situ with reaction) is also addressed in this chapter, presenting several advantages of these promising intensified processes for the sugar industry.
Access this chapter
Tax calculation will be finalised at checkout
Purchases are for personal use only
Similar content being viewed by others
References
Clarke MA (1993) Sugars and nonsugars in sugarcane. In: Chen JCP, Chou C-C (eds) Sugar cane handbook. Wiley, New York, pp 21–39
Vaňková K, Onderková Z, Antošová M, Polakovič M (2008) Design and economics of industrial production of fructooligosaccharides. Chem Pap 62(4):375–381
Robyt JF (1998) Essentials of carbohydrate chemistry, Springer advanced texts in chemistry. Springer, New York
Mitsuiki S, Utsunomiya H, Nakama Y, Sakai M, Mukae K, Moriyama Y, Goto M, Furukawa K (2005) Purification and characterization of maltotriose-producing amylases from an alkaliphilic nocardiopsis sp. Toa-1. J Appl Glycosci 52(2):95–99
Clarke MA (2000) Sugar, cane sugar. Kirk-othmer encyclopedia of chemical technology. John Wiley & Sons, Inc
Coca M, Mato S, González-Benito G, Ángel Urueña M, García-Cubero MT (2010) Use of weak cation exchange resin lewatit s 8528 as alternative to strong ion exchange resins for calcium salt removal. J Food Eng 97(4):569–573
Gryllus V (1967) Verfahren zur regenerierung des ionenaustauschers und zur verringerung des alkali-ionengehaltes von zuckerfabriksabläufen bei der enthärtung von dünnsaft mittels ionenaustausches. AT Patent 258230
Rousseau G (1999) Method of regenerating ion exchange resins in the process of decalcification of sugar factory juices. US Patent 5958142
Mindler AB (1948) Demineralization of sugar cane juice. Ind Eng Chem 40(7):1211–1215. 10.1021/ie50463a010
Massay R (1850) Improvements in defecating sugar. US Patent 7342
Urban K (1925) Improvements in the purification of sugar solutions. GB Patent 240253
Elbogen S (1925) Procédé de purification des solutions sucrées au moyen de silicates ou autres produits artificiels, qui possèdent la propriété d’échanger les alcalino-terreux contre des alcalins des solutions sucrées. FR Patent 584967
Quentin G (1961) Verfahren zur erhoehung der kristallisationsfaehigkeit des zuckers in loesungen der zuckerfabrikation. DE Patent 974408
LaBrie RL, Bharwada UJ (1992) Process for demineralizing a sugar-containing solution. US Patent 5094694
Bakker A, Schepers GJJM, Koerts K (1989) Method for demineralizing beet sugar thin juice. US Patent 4799965
Kouji T, Fumihiko M, Kikuzo K, Makoto T, Takayuki M (2001) Process for demineralizing a sugar solution. US Patent 6224683
Colonna WJ, Samaraweera U, Clarke MA, Cleary M, Godshall MA, White JS (2000) Sugar. Kirk-othmer encyclopedia of chemical technology. John Wiley & Sons, Inc
Broughton DB (1983) Sucrose extraction from aqueous solutions featuring simulated moving bed. US Patent 4404037
Broughton DB (1984) Extraction of sucrose. EP Patent 0103406
Bento LSM (1998) Ion exchange resins for decolorization. Int Sugar J 100(1191):111–117
De Lataillade J, Rousset F (2002) Ion-exchange decolorization: a flexible way to modernization and capacity extension. Int Sugar J 104(1237):5–9
Kunin R (1972) Ion exchange resins. Robert E. Krieger, New York
Coca M, García MT, Mato S, Cartón A, González G (2008) Evolution of colorants in sugarbeet juices during decolorization using styrenic resins. J Food Eng 89(4):429–434
L’Hermine GJA, Lundquist EG (1999) Decolorization of sugar syrups using functionalized adsorbents. US Patent 5972121
Soest H-K, Klipper DR, Schnegg DU, Gladysch M (2005) Sugar juice colour removal using monodispersed anion exchangers. EP Patent 1205560
Bento LR (1991) Processing for regenerating sugar decolorizing ion exchange resins, with regenerant recovery. US Patent 5019542
Bento LR (1998) Process for regeneration of ion-exchange resins used for sugar decolorization, using chloride salts in a sucrose solution alkalinized with calcium hydroxide. US Patent 5932106
Ihm S-K, Oh I-H (1984) Correlation of a two-phase model for macroreticular resin catalyst in sucrose inversion. J Chem Eng Jpn 17(1):58–64
Dooley KM, Gates BC (1984) Superacid polymers from sulfonated poly(styrene-divinylbenzene): preparation and characterization. J Polymer Sci Polymer Chem Ed 22(11):2859–2870
Martin AJP (1949) Summarizing paper. Discuss Faraday Soc 7:332–336
Broughton DB, Gerhold CG (1961) Continuous sorption process employing fixed bed of sorbent and moving inlets and outlets. US Patent 2985589
Uretschläger A, Jungbauer A (2002) Preparative continuous annular chromatography (p-cac), a review. Bioprocess Biosystems Eng 25(2):129–140
Byers CH, Sisson WG, Decarli JP, Carta G (1989) Pilot-scale studies of sugar separations by continuous chromatography. Appl Biochem Biotechnol 20–21(1):635–654
Wolfgang J, Prior A (2002) Continuous annular chromatography. In: Freitag R (ed) Modern advances in chromatography, vol 76, Advances in biochemical engineering/biotechnology. Springer, Berlin/Heidelberg, pp 233–255 10.1007/3-540-45345-8_7
Howard AJ, Carta G, Byers CH (1988) Separation of sugars by continuous annular chromatography. Ind Eng Chem Res 27(10):1873–1882
Byers CH, Sisson WG, DeCarli JP, Carta G (1990) Sugar separations on a pilot scale by continuous annular chromatography. Biotechnol Prog 6(1):13–20 10.1021/bp00001a003
Bart HJ, Messenböck RC, Byers CH, Prior A, Wolfgang J (1996) Continuous chromatographic separation of fructose, mannitol and sorbitol. Chem Eng Process: Process Intensificat 35(6):459–471
Wolfgang J, Prior A, Bart HJ, Messenböck RC, Byers CH (1997) Continuous separation of carbohydrates by ion-exchange chromatography. Sep Sci Technol 32(1–4):71–82
Barker PE, Bridges S (1991) Continuous annular chromatography for the separation of beet molasses. J Chem Technol Biotechnol 51(3):347–359
Takahashi Y, Goto S (1994) Continuous separation of fructooligosaccharides using an annular chromatograph. Sep Sci Technol 29(10):1311–1318
Adam P, Nicoud RM, Bailly M, Ludemann-Hombourger O (2004) Process and device for separation with variable-length chromatographic zones. US Patent 6712973
Zang Y, Wankat PC (2002) Smb operation strategy – partial feed. Ind Eng Chem Res 41(10):2504–2511
Lutin F, Bailly M, Bar D (2002) Process improvements with innovative technologies in the starch and sugar industries. Desalination 148(1–3):121–124
Rajendran A, Paredes G, Mazzotti M (2009) Simulated moving bed chromatography for the separation of enantiomers. J Chromatogr A 1216(4):709–738
Sá Gomes P, Rodrigues AE (2007) Outlet streams swing (oss) and multifeed operation of simulated moving beds. Sep Sci Technol 42(2):223–252
Zhang Z, Mazzotti M, Morbidelli M (2003) Powerfeed operation of simulated moving bed units: changing flow-rates during the switching interval. J Chromatogr A 1006(1–2):87–99
Schramm H, Kaspereit M, Kienle A, Seidel-Morgenstern A (2002) Improving simulated moving bed processes by cyclic modulation of the feed concentration. Chem Eng Technol 25(12):1151–1155
Kim JK, Abunasser N, Wankat PC (2005) Use of two feeds in simulated moving beds for binary. Korean J Chem Eng 22(4):619–627
Mun S (2006) Enhanced separation performance of the simulated moving bed process with two raffinate and two extract products. J Chem Eng Jpn 39(10):1054–1056
Beste YA, Arlt W (2002) Side-stream simulated moving-bed chromatography for multicomponent separation. Chem Eng Technol 25(10):956–962
Mata VG, Rodrigues AE (2001) Separation of ternary mixtures by pseudo-simulated moving bed chromatography. J Chromatogr A 939(1–2):23–40
Borges da Silva EA, Rodrigues AE (2006) Design of chromatographic multicomponent separation by a pseudo-simulated moving bed. AICHE J 52(11):3794–3812
Bieser HJ, deRosset AJ (1977) Continuous counter-current separation of saccharides with inorganic adsorptions. In: Paper presented at the 28th starch convention, Detmold, 27–29 Apr 1977
Giacobello S, Storti G, Tola G (2000) Design of a simulated moving bed unit for sucrose-betaine separations. J Chromatogr A 872(1–2):23–35
Zhang Z, Wang J, Feng Q (2004) Process for separating mannitose and glucose by analog moving bed. CN Patent 1528769
Zhang Z, Wang J, Liu J (2004) High-yield manna sugar preparation process. CN Patent 1528728
Neuzil RW, Priegnitz JW (1980) Process for separating a ketose from an aldose by selective adsorption. US Patent 4226977
Landis AM, Broughton DB, Fickel RG (1981) Simulated countercurrent sorption process employing ion exchange resins with backflushing. US Patent 4293346
Fickel RG (1982) Simulated countercurrent sorption process employing ion exchange resins with periodic backflushing. US Patent 4319929
Landis AM, Broughton DB, Fickel RG (1983) Simulated countercurrent sorption process employing ion exchange resins with backflushing. EP Patent 0075611
Rearick DE, Kearney M, Costesso DD (1997) Simulated moving-bed technology in the sweetener industry. ChemTech 27(9):36–40
Saari P, Häkkä K, Jumppanen J, Heikkilä H, Hurme M (2010) Study on industrial scale chromatographic separation methods of galactose from biomass hydrolysates. Chem Eng Technol 33(1):137–144
Kearney MM, Mumm MW (1991) Chromatographic separator sorbent bed preparation. US Patent 4990259
Kearney MM, Hieb KL (1992) Time variable simulated moving bed process. US Patent 5102553
Kearney MM, Kochergin V, Peterson KR, Velasquez L (1995) Sugar beet juice purification process. US Patent 5466294
Ando M, Hirota T, Shioda K (1980) Adsorption separation method and apparatus therefore. EP Patent 10769
Masuda T, Kawano K, Miyawaki I (1995) Process for production of starch sugars. US Patent 5391299
Tanimura M, Tamura M (1996) Method of separation into three components using a simulated moving bed. US Patent 5556546
Hyöky G, Paananen H, Cotillon M, Cornelius G (1999) Presentation of the fast separation technology. In: Paper presented at the 30th general meeting ASSBT-American Society of Sugar Beet Technologysts, Orlando, 13 Feb 1999
Heikkila H, Hyoky G, Kuisma J (2000) Method for the fractionation of molasses. US Patent 6093326
Hyoky G, Paananen H, Monten K-E, Heikkila H, Kuisma J (1998) Fractionation method of sucrose-containing solutions. US Patent 5795398
Ahlgren BK, Snyder CB, Fawaz I (2004) Fluid-directing multiport rotary valve. US Patent 6719001
Wijnberg BP (2005) Device for carrying out a chemical or physical treatment. WO Patent 2005025738
Evers JA (2006) Rotary distributor valve for chemical/physical treatment of a fluid. WO Patent 2006036062
Theoleyre M-A, Konetzke GDrnDC, Schmidt KDrnDC, Weidemann RDI (2002) Method of preparation of sorbitols from standard-glucose. EP Patent 1176131
Chang C-H (1989) Process for separating psicose from another ketose. EP Patent 0302970
An SC, Jee HS, Doh MH (1998) Process for obtaining, by separation, highly pure water-soluble polydextrose. US Patent 5831082
Antila J, Ravanko V, Walliander P (1998) Method of preparing l-arabinose from sugar beet pulp. WO Patent 1999/010542
Heikkila H, Hyoky G, Kuisma J (1989) Method for the recovery of betaine from molasses. EP Patent 345511
Kikuzo K, Takayuki M, Kohei S, Kouji T, Fumihiko M (2000) Process for recovering betaine. US Patent 6099654
Leão CP, Rodrigues AE (2004) Transient and steady-state models for simulated moving bed processes: numerical solutions. Comput Chem Eng 28(9):1725–1741
Azevedo DCS (2001) Separation/reaction in simulated moving bed. Ph.D. Thesis, University of Porto, Porto
Azevedo DCS, Rodrigues AE (2001) Design methodology and operation of a simulated moving bed reactor for the inversion of sucrose and glucose-fructose separation. Chem Eng J 82(1–3):95–107
Cen P, Tsao GT (1993) Recent advances in the simultaneous bioreaction and product separation processes. Sep Technol 3(2):58–75
Sarmidi MR, Barker PE (1993) Simultaneous biochemical reaction and separation in a rotating annular chromatograph. Chem Eng Sci 48(14):2615–2623
Sarmidi MR, Barker PE (1993) Saccharification of modified starch to maltose in a continuous rotating annular chromatograph (crac). J Chem Technol Biotechnol 57(3):229–235
Meurer M, Altenhöner U, Strube J, Untiedt A, Schmidt-Traub H (1996) Dynamic simulation of a simulated-moving-bed chromatographic reactor for the inversion of sucrose. Starch-Starke 48(11–12):452–457 10.1002/star.19960481113
Minceva M, Rodrigues AE (2005) Simulated moving-bed reactor: reactive-separation regions. AICHE J 51(10):2737–2751
Minceva M, Silva VMT, Rodrigues AE (2005) Analytical solution for reactive simulated moving bed in the presence of mass transfer resistance. Ind Eng Chem Res 44(14):5246–5255
Sá Gomes P, Leão CP, Rodrigues AE (2007) Simulation of true moving bed adsorptive reactor: detailed particle model and linear driving force approximations. Chem Eng Sci 62(4):1026–1041
Hashimoto K, Adachi S, Noujima H, Ueda Y (1983) A new process combining adsorption and enzyme reaction for producing higher-fructose syrup. Biotechnol Bioeng 25(10):2371–2393 10.1002/bit.260251008
Borges da Silva EA, Ulson de Souza AA, de Souza SGU, Rodrigues AE (2006) Analysis of the high-fructose syrup production using reactive smb technology. Chem Eng J 118(3):167–181
Barker PE, Ganetsos G, Ajongwen J, Akintoye A (1992) Bioreaction-separation on continuous chromatographic systems. Chem Eng J 50(2):B23–B28
Bubnik Z, Pour V, Gruberova A, Starhova H, Hinkova A, Kadlec P (2004) Application of continuous chromatographic separation in sugar processing. J Food Eng 61(4):509–513
Glueckauf E (1955) Theory of chromatography. Part 10. Formulae for diffusion into spheres and their application to chromatography. Trans Faraday Soc 51:1540–1551
Acknowledgments
P. Sá Gomes gratefully acknowledges the support from Fundação para a Ciência e Tecnologia, Ministry of Science, Technology and Higher Education of Portugal (postdoc grant ref.: SFRH/BPD/63764/2009).
Author information
Authors and Affiliations
Corresponding author
Editor information
Editors and Affiliations
Annexes
Annexes
5.1.1 Annex (1)
The mathematical model approach, hereby used to simulate an SMB unit, represents it as a sequence of columns described by the usual system equations for an adsorptive fixed bed (each column \( k\)). All these columns are then linked by the so-called node equations, stated to each section \( j\), making use of the equivalence between the interstitial velocity in the TMB and SMB, and thus one has for
Due to the switch of the inlet and outlet lines, the boundary conditions to a certain column are not constant during a whole cycle, but change after a period equal to the switching time. Since the model equations are set to each column \( k\), the concentration of \( i\) species at the beginning of each column \( k\), \( {C}_{{b}_{i,k}}^{0}\), must be recalculated for each switching time period following the next node mass balances:
\( t=0\) to \( {t}_{s}\):
\( t={t}_{s}\) to \( 2{t}_{s}\):
This set of equations continues to progress in a similar way (shifting one column per \( {t}_{s}\)), until \( {\displaystyle {\sum }_{j=I}^{IV}{n}_{j}}{t}_{s}\), repeating then from the first switch.
Considering the dimensionless variables \( x=\frac{z}{{L}_{c}}\) and \( \theta =\frac{t}{{t}_{s}}\), and a linear driving force (LDF) approximation [95] to the mass transfer (set in terms of the adsorbed phase in equilibrium with the bulk concentration and the average adsorbed phase concentration: \( {a}_{i,k}\left({q}_{i,k}^{eq}-\langle {q}_{i,k}\rangle \right)\), where \( {a}_{k}={k}_{LDF}{t}_{k}\)), one can establish a set of mass balances equations for each species \( i\) in each column \( k\), in each section \( j\), as follows for the bulk fluid phase:
and for the mass balance in the particle,
with the respective initial:
and boundary conditions:
where \( {g}_{j}^{*}=\frac{{u}_{j}^{*}}{{u}_{s}}\) is the ratio between SMB fluid and the solid interstitial velocities and \( P{e}_{j}^{*}=\frac{{u}_{j}^{*}{L}_{c}}{{D}_{b}}\) the column Peclet number. As consequence, one obtains discontinuous solutions, reaching not a continuous steady state (SS) but a cyclic steady state (CSS).
5.1.1.1 Performance Parameters
The definitions of purity and recovery of these performance parameters, for the case of a binary mixture, are given below:
Purity (%) of the more retained (A) species in extract and the less retained one (B) in the raffinate streams, over a complete cycle (from \( q\) to \( q+{\displaystyle {\sum }_{j=I}^{IV}{n}_{j}}\)):
Recovery (%) of more retained (A) species in extract and the less retained one (B) in raffinate streams, again over a complete cycle:
5.1.2 Annex (2)
As mentioned before, the JO process (or Pseudo-SMB) is characterized by a discontinuous operating mode, mainly divided into two major steps. The mathematical model to simulate such process also replicates such discontinuity.
Step 1 (from 0 to \( {t}_{Step1}\))
During step 1, the feeding is performed and the intermediary product is purged, as mentioned, before leading to the node balances:
and for each species \( i\):
with \( {u}_{j}^{1*}\) representing interstitial velocity in section \( j\)during step 1.
Within each column, the concentration profiles are simulated by means of the well-known fixed-bed equations, initial and boundary conditions, similar to those expressed for the LDF approach for each column in the SMB modeling strategy (see Annex 1).
Step 2 (from \( {t}_{Step1}\) to \( {t}_{Step2}\))
In the second operation stage (step 2), one has the following nodes balances:
and for each species \( i\):
During step 2, similar mass balances and boundary conditions stated for the classical SMB unit (Annex 1) are used to simulate the operation of the Pseudo-SMB unit.
5.1.2.1 Performance Parameters (Pseudo-SMB)
The definitions of extract, intermediary, and raffinate purities (\( P{U}_{X},P{U}_{It},P{U}_{R}\), %) and recovery at the extract, intermediary, and raffinate ports (\( R{E}_{X},R{E}_{It},R{E}_{R}\), %) of the more intermediary and less retained components, respectively, are stated as follows:
Component A (during step 2):
, during Step 2
Component B (during step 1):
Component C (during step 2):
Rights and permissions
Copyright information
© 2012 Springer Science+Business Media B.V.
About this chapter
Cite this chapter
Silva, V.M.T.M., Gomes, P.S., Rodrigues, A.E. (2012). Use of Ion Exchange Resins in Continuous Chromatography for Sugar Processing. In: Inamuddin, D., Luqman, M. (eds) Ion Exchange Technology II. Springer, Dordrecht. https://doi.org/10.1007/978-94-007-4026-6_5
Download citation
DOI: https://doi.org/10.1007/978-94-007-4026-6_5
Published:
Publisher Name: Springer, Dordrecht
Print ISBN: 978-94-007-4025-9
Online ISBN: 978-94-007-4026-6
eBook Packages: Chemistry and Materials ScienceChemistry and Material Science (R0)