Industrial Results:
1. Fructose/ Dextrose Separation:
This chromatographic separation has the highest number of installations
worldwide and features, with the ISMB process, the following performances
depending on the design parameters. The DIAION® UBK resins are
used in the calcium form.
Feed Product (Fructose) Rafinate (Dextrose) Recovery Rate FRUCTOSE
43.0% 94.4% 3.8% 95.0% DEXTROSE 52.0% 4.0% 88.9% OTHER 5.0% 2.0%
7.3% TDS (Bx) 60.0% 36.0% 28.0% Feed Product (Fructose) Rafinate
(Dextrose) Recovery Rate FRUCTOSE 44.0% 97.0% 6.7% 91.0% DEXTROSE
51.2% 1.0% 86.5% OTHER 4.8% 2.0% 6.8% TDS (Bx) 60.0% 36.0% 24.4%
2. Separation Sugars - Non-sugars:
The first ISMB unit in Europe has been in operation for two years
with a Fructose syrup. The investment was decided, among other
reasons, to increase the capacity of an existing ion exchange
resin system without significantly increasing the polluting load.
Feed syrup:
- Decalcified Fructose syrup
- Bx: 60
- Fructose purity:85 %
- Temperature: 65ºC
PH =5 Performances:
- Purity of Product fraction =96.0%
- Recovery rate =98.5%
- Removal of non-sugars =75%
- W/F 3
- Volumetric load 0.105 l/ l.h
- Energy consumption 1.7 kWh/m3
The UBK resin is used in the sodium form. Schematics 7 and 8 show
the feed/ removal and recirculation sequences.
SCHEMATICS FEED/ REMOVAL RECIRCULATION
Assuming that the required specifications for the syrup and the
elution water are met, the ISMB process can globally operate 350
days/ year. For such a continuous operation, two annual stoppages
are suggested to define columns/ chambers in which the pressure
drop does not exceed an average of 3 bars. Softened water or condensate
suitably filtered at 25 microns is used for the elution. The decalcified
syrup feed (with a monovalent to divalent ratio of 50) is also
filtered at the same cut-off point.
Conclusion:
The ISMB chromatography process used for the Fructose/ Dextrose
separation with resins in the calcium form and for the sugar (Fructose)
/ non-sugar separation with resins in the sodium form features
high performances.
These includes:
- A higher volumetric load compared the SMB system and, therefore,
a lower volume of resins by approx. 30 %;
- A lower water consumption with a W/F ratio of approx. 1.8
and 3, respectively;
- A lower energy consumption thanks to the operating mode
and smaller pressure drops across the distributors/ collectors
and the resin beds.
As a result, the smaller dimensions for the columns/ chambers
and the simplification of the auxiliary equipment (such as valves,
pipes, pumps, instrumentation, etc.) both contribute to make the
investment for ISMB chromatography processes very competitive.
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