Mass‐transfer effects on the rate of isomerization of <scp>D</scp>‐glucose into <scp>D</scp>‐fructose, catalyzed by whole‐cell immobilized glucose isomerase

Boersma, Jan; Vellenga, K.; Wilt, H.G.J. de; Joosten, G.E.H.

doi:10.1002/bit.260211003

Cited by 27 publications

(12 citation statements)

References 11 publications

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“…Furthermore, in Table 1 , beads with 0.8 mm size have higher yield than 2 mm type at all flow rate and glucose concentration due to reduction of intra-phase mass transfer limitations. Reduction in size of beads until no longer intra-phase mass transfer limitations exists, enhances the ethanol productivity which was also observed by (Duarte et al 2013 ; Pilkington et al 1998 ; Boersma et al 1979 ). Furthermore in both types of beads, the addition of glucose has also been observed to have an effect on the ethanol productivity that might be due to increased substrate diffusional resistance and development of concentration gradient.…”

Section: Discussionsupporting

confidence: 59%

Operational parameters and their influence on particle-side mass transfer resistance in a packed bed bioreactor

et al. 2015

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The influence of internal mass transfer on productivity as well as the performance of packed bed bioreactor was determined by varying a number of parameters; chitosan coating, flow rate, glucose concentration and particle size. Saccharomyces cerevisiae cells were immobilized in chitosan and non-chitosan coated alginate beads to demonstrate the effect on particle side mass transfer on substrate consumption time, lag phase and ethanol production. The results indicate that chitosan coating, beads size, glucose concentration and flow rate have a significant effect on lag phase duration. The duration of lag phase for different size of beads (0.8, 2 and 4 mm) decreases by increasing flow rate and by decreasing the size of beads. Moreover, longer lag phase were found at higher glucose medium concentration and also with chitosan coated beads. It was observed that by increasing flow rates; lag phase and glucose consumption time decreased. The reason is due to the reduction of external (fluid side) mass transfer as a result of increase in flow rate as glucose is easily transported to the surface of the beads. Varying the size of beads is an additional factor: as it reduces the internal (particle side) mass transfer by reducing the size of beads. The reason behind this is the distance for reactants to reach active site of catalyst (cells) and the thickness of fluid created layer around alginate beads is reduced. The optimum combination of parameters consisting of smaller beads size (0.8 mm), higher flow rate of 90 ml/min and glucose concentration of 10 g/l were found to be the maximum condition for ethanol production.

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Section: Discussionsupporting

confidence: 59%

Operational parameters and their influence on particle-side mass transfer resistance in a packed bed bioreactor

et al. 2015

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“…where vm and km are apparent rate constants and both can have negative values [4,5,10]. k~ is a function of temperature and initial substrate concentration So.…”

Section: Vp K S )mentioning

confidence: 99%

“…Most of the published work on GI reactor are about developing kinetic equation for the immobilized enzyme [2,3,4]. Little is published about the effect of temperature on the reaction kinetics [5) 6] and reactor performance and very few papers considered the effect of substrate protection [7,8,9].…”

Section: Introductionmentioning

confidence: 99%

Simulation of glucose isomerase reactor: optimum operating temperature

Abu-Reesh

Faqir

1996

Bioprocess Engineering

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“…Therefore in our laboratory systematic investigations have been carried out into the stability of an immobilized whole cell glucose isomerase catalyst, the initial kinetics of which we investigated before (Boersma et al, 1979;Kikkert et al, 1981; Van Keulen et al, 1981). In the catalyst used the glucose isomerase is immobilized within the cells while the cells are immobilized as well ( Van Keulen et al, 1981).…”

Section: Introductionmentioning

confidence: 99%

“…Overall, the isomerization reaction may be considered to comprise the following steps (Boersma et al, 1979): (a) substrate transfer from the bulk of the liquid to the external surface of the catalyst particles, (b) substrate transfer to the cells through the pores of a particle, (c) substrate transfer through the wall and membrane of an Arthrobacter cell, (d) substrate transfer to the intracellular glucose isomerase, (e) reversible isomerization of glucose into fructose, and (f)-(i) product transfer from the enzyme to the bulk of the liquid.…”

Section: Introductionmentioning

confidence: 99%

Isomerization of glucose to fructose. 1. The stability of a whole cell immobilized glucose isomerase catalyst

Straatsma¹,

Vellenga²,

Wilt³

et al. 1983

Ind. Eng. Chem. Proc. Des. Dev.

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Ind. Eng. Chem. Process Des. Dev. 1983, 22, 349-356 349 Guln, J. A.; Tarrer, A. R.; Lee, J. M.; Lo, L.; Curtls, C. W. Ind. Eng. Chem. Process Des. Dev. 1979, 18, 371. Guln, J. A.; Tarrer, A. R.; Lee, J. M.; Van Brackle, H. F.; Curtis, C. W. Ind. Eng. Chem. Process Des. Dev. 1970, 18, 631. Guin, J. A.; Lee, J. M.; Fan, C. W.; Curtis, C. W.; Lloyd, J. L.; Tarrer, A. R. Ind. Eng. Chem. Process Des. Dev. 1980, 19, 440. Hung. W. J.; Curtis, C. W.; Guin, J. A.; Clinton, J. H.; Barwood, H. L.; Tarrer, A. R. Paper 6d presented at Sprlng National AlChE Meetlng, Houston, TX, 1981a. Hunag, W. J.; Smith, N. L.; Guin, J. A.; Curtis, C. W.; Tarrer, A. R. Presented at 74th Annual AlChE Meeting, New Orleans, LA 1981b. Lambert. J. M.; Slmkovlch, 0.; Walker, P. L. Fuel 1980, 59, 687. Lowry, H. H., Ed. "Chemlstry of Coal Utilizatlon", Supplementary Volume; Wlley: New York; 1963; p 265-268. MazzOCco, N. J.; Klunder, E. 8.; Krastman, D. Pittsburgh Eng. Tech. Center, Phburgh, PA, Report No. DOE/PETC/Tl?-81/1, March 1981. Montano, P. A.; Granoff, B. Fuel 1980. 59. 214. Moroni, E. C. Paper 8a presented at Sprlng AIChE Meeting, Houston, TX, 1981. Neavei, R. C. Fuel 1976, 55, 237. Neavel, R. C. Phil. Trans. R . Soc. Lond. 1981. A300. 141. Orchin, M.; Storch, H. H. Ind. €ng. Chem. 1948, 40, 1385. Raaen, V. F.; Roark, W. H. Fuel 1978, 57. 650. Sapre, A. V.; Gates, B. C. Ind. €ng. Chem. Process Des. Dev. 1981, 20, Thomas, M. G.; Padrlck, T. D.; Stohi, F. V. Sandla Lab. Report SAND-80-Varghese, P.; Derbyshke, F. J.; Whltehurst, D. C. Paper 6b presented atThe rate of deactivation of an immobilized whole cell Arthrobacter glucose isomerase catalyst has been determined quantitatively as a function of a number of parameters. The deactivation is most senskive to pH and temperature, while other possible parameters, such as oxygen concentration, byproduct Concentration, and impurities present in a synthetic feed stream, appeared to have only a minor Influence on the rate of deactivation under normal process conditions. The deactivation is probably caused by denaturation of the enzyme and not by mechanisms such as proteolysis, change of the membrane structure of an Arthrobacter cell, or pore plugging.

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Mass‐transfer effects on the rate of isomerization of D‐glucose into D‐fructose, catalyzed by whole‐cell immobilized glucose isomerase

Cited by 27 publications

References 11 publications

Operational parameters and their influence on particle-side mass transfer resistance in a packed bed bioreactor

Operational parameters and their influence on particle-side mass transfer resistance in a packed bed bioreactor

Simulation of glucose isomerase reactor: optimum operating temperature

Isomerization of glucose to fructose. 1. The stability of a whole cell immobilized glucose isomerase catalyst

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