Open Access

Purification of DP 6 to 8 chitooligosaccharides by nanofiltration from the prepared chitooligosaccharides syrup

  • Huizhong Dong1, 2,
  • Yaosong Wang1, 2,
  • Liming Zhao1, 2Email author,
  • Jiachun Zhou1, 2,
  • Quanming Xia1, 2,
  • Lihua Jiang1, 2 and
  • Liqiang Fan1, 2
Bioresources and Bioprocessing20141:20

DOI: 10.1186/s40643-014-0020-x

Received: 13 July 2014

Accepted: 14 October 2014

Published: 19 November 2014



Chitooligosaccharides (COS) with degrees of polymerization (DP) 6 to 8 are degraded from chitosan, which possess excellent bioactivities. However, technologies that could purify them from hydrolysis mixtures in the narrow DP range (984 to 1,306 Da) are absent. The objective of this research is to purify DP 6 to 8 COS by nanofiltration on the basis of appropriate adjustments of the feed condition.


Syrup containing DP 6 to 8 COS at different concentrations (19.0 to 46.7 g/L) was prepared. A commercial membrane (QY-5-NF-1812) negatively charged was applied. Experiments were carried out in full recycle mode, so that the observed COS retentions were investigated at various transmembrane pressures (6.0 to 20.0 bar), temperatures (10°C to 50°C), and pHs (5.0 to 9.0). Then, the feasibility of separation of DP 6 to 8 COS was further studied by concentration ratio under optimum conditions.


The results indicate that the purification of DP 6 to 8 COS by nanofiltration NF is feasible. It was found that the permeate flux was 95.0 L/(m2 h) at 10.0 bar, while it reached to 140.0 L/(m2 h) at 20.0 bar, and it increased with feed temperature, but the membrane pores were also swelled by heating and led to an irreversible wastage of target oligomers. Additionally, the retention behaviors of chitooligosaccharides are significantly influenced by pH.


Although glucosamine and dimer were permeatable at low pH, their retention ratios were remarkably varied from 0.458 to 0.864 when pH was 9.0. With the interaction of hydrogen bonds, structural curling and overlapping of chitooligosaccharides were formed. Consequently, the rejection of chitooligosaccharides at various pHs is variable. Spray-dried products were finally characterized by the matrix-assisted laser desorption/ionization time-of-flight mass spectrum. The spectrum identified the distributions of hexamer, heptamer, and octamer. Combined with high-performance liquid chromatography profiles, the purity and yield of DP 6 to 8 chitooligosaccharides were up to 82.2% and 73.9%, respectively.


Nanofiltration Chitooligosaccharides Degree of polymerization Separation MALDI-TOF-MS

1 Background

Chitooligosaccharides (COS) are defined as the partially degraded products of chitosan or low-molecular-weight chitosan (LMWC) with a degree of polymerization (DP) ranges from 2 to 20 [1]. As shown in Figure 1, their molecular structures are linear oligosaccharides composed of 2-amino-2-deoxy-D-glucopyranose and 2-acetamino-2-deoxy-D-glucopyranose (Figure 1(A)) units which are linked by β(1 → 4) glycosidic bonds [2].
Figure 1

Molecular structures of glucosamine and DP 3 chitooligosaccharide. Structurally, chitooligosaccharides, including glucosamine and trimer, are linear oligosaccharides composed of 2-amino-2-deoxy-D-glucopyranose and 2-acetamino-2-deoxy-D-glucopyranose units which are linked by β(1 → 4) glycosidic bonds. (A) The molecular structure of glucosamine. (B) The molecular structure of DP 3 chitooligosaccharide.

According to many previous reports, COS possess a series of attractive bioactive properties, including antibacterial [3], anticoagulant [4], antimicrobial [5], antioxidant [6], anticancer [7], hypolipidemic [8], and immune-stimulating [9] effects. Based on these excellent advantages mentioned before, COS are responsible for practical applications in beverage processing [10], functional ingredients [11], and biomedicines [12], which are different from chitosan and chitin except for their contributions on food packaging [13]. Nowadays, hybrid enzymatic hydrolysis has become the ideal technology for COS preparation due to its high efficiency and little structural modification [14]. Unfortunately, the products after enzymatic degradation were just intermediate ones [15]. Suitable methods should be used to separate target COS from mixtures coexisting in the solution, such as the high molecular weight of chitosan, proteins (enzymes), and inorganic salts.

Conventionally, COS is purified by various chromatographies. Fan et al. succeeded in obtaining COS by macroporous resins from fermentation broth, and the productivity of target products could go up to 90% (w/w) under optimum conditions [16]. Meanwhile, Cabrera and Custem reported that the concentrations of COS could be analyzed by matrix-assisted laser desorption/ionization time-of-flight mass spectrum (MALDI-TOF-MS) [17]. Although the chromatography technology is feasible to remove irrelevant components and refine COS in terms of DP, it is only accepted in laboratory analysis but far from scale-ups. In practice, several negative problems inevitably appear during continuous using of chromatography, including the demands on cleaning and regeneration of column packing, adsorption capacities of COS, and relatively high production cost [18],[19].

Recently, there is a growing attention on nanofiltration (NF) applications, especially for COS preparation. Kim et al. reported that several instruments were used to prepare COS, the details of which could be summarized in immobilized enzymatic columns and ultrafiltration (UF) membrane reactors [2]. Han et al. demonstrated the desalination feasibility of NF-40 membrane for chitobiose solution. Under acidic conditions, the interception of solutes ranks as chitobiose > glucosamine > Na+ > H+[20]. Furthermore, the steric and electrostatic effects are inferred according to the sequence. Han et al. also studied the influence of three membranes (DL, DK, NTR-7540) on COS separation and drew identical conclusions [21]. In a word, NF has been proved to be an effective technology for the separation and purification of COS.

Chitosan was originally hydrolyzed by enzymes, which resulted in the coexistence of various DP COS, glucosamines, and salts. It is evident that there is a great difference in molecular weight among the solutes. Also, the wider ranges of hydrolysis products make it difficult to improve the purity and yield of COS. For instance, DP 6 to 8 COS (984 to 1,306 Da) plays an important role in cancer curing [22]. Therefore, this study is to investigate the separation performance of DP 6 to 8 COS at different solution properties and present a promising purification technology by NF.

2 Methods

2.1 Materials

The raw syrup containing DP 6 to 8 COS was made from chitosan by enzymatic hydrolysis. Chitosan was supplied by Yunzhou Biochemistry Co., Ltd. (Shandong, China). The enzyme mixture (chitosanase from Streptomyces griseus - EC; cellulase from Trichoderma - EC was obtained from Golden-Shell Biochemical Co. (Zhejiang, China). DP 2 to 8 COS and glucosamine standards were purchased from Huicheng Biochemical Co., Ltd. (Shanghai, China). All chemicals used in the NF operation and high-performance liquid chromatography (HPLC) analysis were analytical grade or chromatographic grade, respectively. Deionized water (conductivity <3.0 μs/cm) for membrane cleaning was produced by ion exchange.

2.2 Preparation of chitooligosaccharide syrup

Chitosan (91.5% degree of deacetylation) was dissolved in acetic acid (1%, w/v) with stirring, and pH was adjusted to 5.3, and then kept at 45°C. The chitosan concentration was 5% (w/v). Combined enzymes (75 U/g) based on chitosan were added into the chitosan solution and hydrolyzed for 6 h, and then, the hydrolysis was terminated by immersion in a boiling water bath. Finally, a UF membrane module (QY-3-UF-1812, AMFOR Inc., Newport Beach, US) was applied to remove enzymes at 50°C. After cooling to ambient temperature, the syrup was diluted to various concentrations for NF separation.

2.3 Membrane

Purification experiments were operated in a pilot setup (Figure 2). The setup composes of a feed tank, a high-flux pump, a membrane vessel, and a flowmeter. Moreover, the inlet and outlet pressures were metered by two pressure gauges, and the feed temperature could be regulated by a circulating cooling water system surrounding the feed tank.
Figure 2

Brief scheme of the nanofiltration system. Purification experiments were operated in batch equipment for laboratory use. V1 to V4 were represented as valves, and P are pressure gages.

The membrane module employed was an organic polymer composite with spiral-wound structures (QY-5-NF-1812, AMFOR Inc., Newport Beach, US). The membrane module is measured as 1.8 in. (4.6 cm) in section diameter and 12 in. (30.5 cm) in length, which is so-called 1812 type module. Also, it is measured by an approximate molecular weight cut-off (MWCO) of 500 Da, which is close to the molecular weight of DP 4 COS. As described in Table 1, the membrane is negatively charged that can tolerate a maximum pressure up to 25.0 bar. The effective surface area is 0.2 m2. The temperature and pH tolerance range cover from 0°C to 60°C and 4 to 12, respectively.
Table 1

Information of NF membrane module

Membrane index





Organic polymers

Filtration area (Am)

0.2 m2


500 Da


0°C to 60°C


4 to 12


<25.0 bar

2.4 Membrane permeate flux

In this study, the permeate flux is represented as the average one in process. The average permeate flux (Jv) is calculated by Equation 1, as follows:
J v = V p A m × t

where Jv is the average permeate flux of the membrane [L/(m2 h)]; Vp is the volume of permeate accumulated in testing time (L); Am is the effective areas of membrane (m2); t is the testing time (h).

2.5 Observed retention ratio

Retention ratio is also one of the most important factors in membrane separation. The observed retention ratio is described by Equation 2:
R obs = 1 C p C b

where Robs is the observed retention ratio of solute (%); Cp is the concentration of solute in the permeate (mol/L); Cb is the concentration of solute in the feed (mol/L).

2.6 Full recycle mode of NF

Initially, 5.0 L raw syrup was added, and the recycling flow rate was adjusted to 360 L/h, which represented the optimum rotation condition for the working pump. The effects of transmembrane pressure (TMP), operation temperature, and pH on NF performance were successively carried out. All the permeate were flowed back to the feed tank, while the Jv and retention behaviors of DP 6 to 8 COS at different concentrations were measured after the renewed conditions were stable for 15 min. It is worth being noted that two of the parameters mentioned must be constant when the third is variable. During the process, the temperature was controlled at 50°C ± 2°C by a heat exchanger surrounding the feed tank, except for the experiments to investigate the effects of temperature on the NF retention on DP 6 to 8 COS.

2.7 Purification of DP 6 to 8 chitooligosaccharides

Purification experiments for DP 6 to 8 COS were executed in batch mode. Under the optimized conditions obtained from the preliminary experiments, the concentrate stream was circulated back to the feed tank, whereas the permeate was collected individually. Considering the practical capacity of the feed tank, 7.0 L of diluted syrup (Cb = 19.0 g/L) was added firstly. Every 1.0 L of extra diluted syrup should be supplied as soon as the permeate was equally removed. Certainly, the systematic temperature during NF was maintained by cooling water. After adding all the syrup (16.0 L), the process was terminated until the volume of permeate reached 14.0 L (2.0 L syrup left in the tank). The effect of the concentration ratio on the purity of DP 6 to 8 COS was confirmed by flux and rejections.

2.8 HPLC analysis

The concentrations of glucosamine and DP 2 to 8 COS were analyzed by an HPLC system (Shimadzu 10A, Shimadzu, Kyoto, Japan) equipped with a high-performance sugar column (Shodex Asahipak NH2P-50 4E, Shodex, Kyoto, Japan) and an RI detector. The mobile phase consists of methyl cyanide and pure water with the ratio of 70:30 (v/v). The column temperature was maintained at 30°C, and the flow velocity was kept at 1.0 mL/min. All the solutes were measured in the form of single-arranged peaks. In general, the glucosamine was firstly eluted, and then, the dimer and trimer were sequentially characterized due to the adsorption strength difference to the stationary phase. The distributions of COS were quantified by integrating peak areas.

2.9 MALDI-TOF-MS analysis

MALDI-TOF-MS analysis of COS was carried out using Shimadzu AXIMA Performance matrix-assisted laser desorption/ionization time-of-flight mass spectrometry (Shimadzu, Kyoto, Japan). All spectra were measured in the reflector mode by external calibration. The laser was scanned at a scale from 500 to 1,500 Da. An aqueous solution of 2,5-dihydroxybenzoic acid (DHB, 100 mg/mL) was used as the matrix.

2.10 Statistical methods

All parameters and experimental results were obtained with means ± SD of parallel tests. The data was analyzed by Statistix 9.0 software (Analytical Software, Tallahassee, FL, USA).

3 Results and discussion

3.1 Characterization of chitooligosaccharide syrup

As the raw material for NF process, the COS syrup was defined as the permeate of UF that was pretreated after enzymatic hydrolysis. Summarized by the previous tests, 10.0 L of chitosan hydrolysates were prepared and purified by UF, while a 2.0-L concentrate and 8.0-L permeate were separately bulked at each concentration level due to the cross-flow filtration mode.

Table 2 shows that the principle components of COS syrup varied with the changeable concentrations of chitosan (1.0% to 5.0%, w/w) after UF. It demonstrated that most of the target products permeated through the UF membrane, while the blocking layer adhered to by macromolecular solutes was slightly affected. However, there was still a little amount of proteins (Cprotein = 1.4 to 2.9 mg/L) that remained, which was partially caused by the temperature effect and concentration polarization. Besides the protein content in the purified syrup, its calculation data was in good agreement with the Robs during the UF process, which was scaled from 0.996 to 0.998 (the data was not shown). The phenomenon suggested that the tested UF membrane was sensitive to the protein rejections.
Table 2

T he component analysis of raw materials for the NF process

Chitosan (%)

Total Proteinsa(mg/L)


DP 6 to8 chitooligosaccharidesa(g/L)


1.4 ± 0.3

0.4 ± 0.1

9.6 ± 1.2


2.7 ± 0.2

0.9 ± 0.1

19.0 ± 1.5


3.3 ± 0.4

1.4 ± 0.2

28.3 ± 1.7


2.9 ± 0.3

1.8 ± 0.2

37.6 ± 2.4


1.4 ± 0.3

2.3 ± 0.4

46.7 ± 2.1

aThe data were determined by three parallel measurements.

In addition, with the increment of crude concentration (Cchitosan), the contents of glucosamine (Cs) and DP 6 to 8 COS (CDP 6 to 8) were also dramatically increased. For example, Cg and CDP 6 to 8 at Cchitosan = 2.0% were 0.9 and 19.0 g/L, respectively, while those at Cchitosan = 5.0% changed to 2.3 and 46.7 g/L, respectively. The tendency indicates that the preparation and separation process of DP 6 to 8 COS was rarely affected by the syrup concentration. According to the data listed in Table 2, the conclusion could be drawn that the purification of hydrolysates by the UF membrane was highly performed. What is more important, the excellent elimination of unexpected impurities may greatly benefit for the next NF treatments.

3.2 Effects of transmembrane pressure on permeate flux

Figure 3 illustrates that the permeate fluxes (Jv) of COS syrup at different Cchitosan increase with the TMP from 6.0 to 20.0 bar. Moreover, it shows a linear relationship between TMP and Jv. For instance, the Jv was 95.0 L/(m2 h) at 10.0 bar for the 9.6-g/L COS solution, whereas it elevated to 122.0 and 140.0 L/(m2 h) at 16.0 and 20.0 bar at the same syrup concentration, respectively. Membrane compaction reduces the mass transfer resistance and enhances the velocity on membrane surface, and thus, leads to an increasing permeate volume of feed solution in regular intervals.
Figure 3

TMP vs. J v of chitooligosaccharide syrup at 50°C during NF separation. Jv of chitooligosaccharide syrup with different Cchitosan ranged by transmembrane pressure (6.0 to 20.0 bar). The permeate fluxes increased with the pressure, whereas they decreased with the increasing concentration of DP 6 to 8 chitooligosaccharides.

Conversely, Jv decreased with the increment of concentration of DP 6 to 8 COS. It could be well explained by the interaction of TMP and the accumulation effects. On the one hand, the solutes would be greatly accumulated by the driving pressure, which is beneficial for the formation of cake layer around the boundary of the membrane. As a result, the membrane pore would be partially blocked and result in a decrement of Jv. On the other hand, the concentration polarization was also exacerbated with the increase of the sugar concentration. When the osmotic pressure was 16.0 bar, Jv declined from 108.0 to 67 L/(m2 h), although the concentration of filtrated syrup ascended from 19.0 to 46.7 g/L.

3.3 Effects of TMP on Robsof DP 6 to 8 COS

As shown in Figure 4, the retentions of DP 6 to 8 COS varied with the TMP, and the Robs of target oligosaccharides were significantly affected by the density and pressure applied. The influence of feed concentration on separation behaviors was emphasized at 28.3 g/L. Due to the existence of DP 6 to 8 COS, the increased concentrations were inevitably brought to a higher permeation of solutes. However, it was also found that the retention coefficient of DP 6 to 8 COS was immobile at higher-pressure areas (18.0 to 20.0 bar). The details could be explained by the steric hindrance interaction between solutes and membrane pores.
Figure 4

TMP vs. R obs of DP 6 to 8 chitooligosaccharides at 50°C during NF separation. It pictured the retentions of DP 6 to 8 chitooligosaccharides when the TMP was set between 6.0 and 20.0 bar. The Robs of DP 6 to 8 chitooligosaccharides were significantly judged by viscosity and pressure applied.

Additionally, the Robs of DP 6 to 8 COS increased with TMP, which indicate that the concentration polarization was a subordinate factor for the separation conditions in this case. As an alkaline molecule, the rejection properties of COS are significantly affected by the Donnan effects [23]. When the concentration was kept at 28.3 g/L, the Robs of solute decreased with the decrease of the pressure (6.0 to 16.0 bar). According to the Donnan theory, dielectric exclusion impels the increasing sugar accumulation, which is responsible for the considerable Robs of DP 6 to 8 COS. Therefore, it could be seen that the dropping of observed retention at a high-pressure range (18.0 to 20.0 bar) was similar. The corresponding results were of the same order with reported phenomena by Zhang [24]. Impressive retention proportions of DP 6 to 8 COS at all selected concentrations and applied pressures were performed.

3.4 Effects of operation temperature on permeate flux

Figure 5 illustrates the experimental data of membrane fluxes over operation temperature, as well as the concentration variations of DP 6 to 8 COS. It hypothesized that the syrup concentration was a constant and that the permeate flux during full recycle mode in the NF separation process was proportional to the temperature, which resulted from membrane swelling and the decrease of syrup viscosity under elevated temperature. As shown in Figure 5, the permeate flux was 79.0 L/(m2 h) at 25°C when the concentration was set at 28.3 g/L. After the temperature rose to 40°C, the permeate flux was correspondingly reached to 89.0 L/(m2 h).
Figure 5

Temperatures vs. J v of chitooligosaccharide syrup at 16.0 bar in NF process. It depicted the effects of Jv on operation temperature, as well as the concentration variations of DP 6 to 8 chitooligosaccharides. Membrane pores were stretched by thermal expansion at high temperature, which reduced the rate of concentration polarization and improved the membrane flux.

To be detailed, the membrane pores were stretched by structural modification when thermal expansion was interposed by external temperature. At the same moment, the increment of temperature meant for a decline of solution viscosity but a rise both in Reynolds number (Re) and mass transfer coefficient (k). Followed by the rules analyzed above, all solutes in the process preferred to move to the bulk part of the syrups, which reduced the rate of concentration polarization and thus improved the membrane flux.

However, excessive temperature was negative to preserve the stability of DP 6 to 8 COS. Because of the special structures that the amino group locates on C-2 sites in every monomer unit linked by β (1 → 4) glycosidic bonds, the velocity of the Maillard reaction was motivated by high temperature. Certainly, further studies are needed to understand the mechanism of the Maillard reaction and its derivative products in permeate during the filtration process.

3.5 Effects of operation temperature on Robsof DP 6 to 8 COS

The retention manners of DP 6 to 8 chitooligosaccharides in different concentrations of syrup are shown in Figure 5, as the temperature varied from 10°C to 50°C. As expected, the retentions of DP 6 to 8 chitooligosaccharides decreased with the increment of temperature. All curves coincide with the conclusion drawn from Figure 5. That is, the thermo swelling of membrane structures promoted more DP 6 to 8 chitooligosaccharides permeated through the NF membrane from the concentrate side. Specifically, the Robs of DP 6 to 8 chitooligosaccharides was 0.912 in 20°C, whereas it diminished to 0.895 at 50°C with the concentration of 37.6 g/L. The transformation was apparently introduced that the Robs of solutes decreased with a boosting temperature that forced the fluid properties of chitooligosaccharide syrup to be a Newtonian liquid and hence resulted in a decrease in viscosity.

Besides, it is also worth noting that the charge effect shifted to become a major factor in the retention behaviors of DP 6 to 8 COS at variable concentrations (Figure 6). Under the same condition (i.e., TMP and temperature), the Robs of hexamer, heptamer, and octamer summed to 0.994 at a concentration of 9.6 g/L, but it declined to 0.874 at a concentration of 46.7 g/L. That could be explained by the Donnan steric pore model (DSPM) theory assumed by Bowen et al. [25]. Given that the negative charges were evenly distributed inside the selected membrane (QY-5-NF-1812), all of the opposite-charged ions as H+ and NH4+ in the solution would be attracted thus the transport of COS was facilitated. Overall, the Jv and retention trends were both restricted by the concentration of syrup and its operation temperature.
Figure 6

Temperatures vs. R obs of DP 6 to 8 chitooligosaccharides at 16.0 bar in NF process. It reflected the retention behaviors of DP 6 to 8 chitooligosaccharides in different concentrations when the temperature varied from 10°C to 50°C. The retentions of DP 6 to 8 chitooligosaccharides decreased with the temperature increased.

3.6 Effects of pH on Robsof COS

The effects of pH ranged from 5.0 to 9.0 on rejections of glucosamine and DP 2 to 8 COS were investigated. Singles situated in the area of 13.0 to 19.0 min represent COS within DP 6 to 8. As shown in Figure 7, the Robs of COS increased with pH, especially for the monomer, dimer, trimer, and tetramer. In the chromatogram of NF concentrate at pH 5.0, it was found that nearly all of COS (DP ≤4) had permeated through the membrane, whereas higher DP were effectively rejected. On the contrary, when the syrup was adjusted to a basic condition (pH = 9.0), the Robs of the monosaccharide and disaccharides arrived at 0.458 and 0.864, respectively, even that the trimer and tetramer completely escaped from the permeate. The reason for this phenomenon might be due to the inter- and intramolecular hydrogen bonds, which further resulted in the unequal curling and overlap in structures. Similar results on Robs and inference for COS have been taken by Han et al. [20]. The stability of the primary structure was broken by hydrogen bonds and restabilized spontaneously. During the recombination process, the curling extent would extremely impact the viscosity and stereospecific blockage of molecules. The structural explosion guided the poor affinity of solutes with the membrane and led to a high resistance of permeation. Furthermore, the rejections of DP 6 to 8 COS, formulated from the concentrate and permeate profiles, were scarcely impacted via pH options (Figure 7). The results indicated that the applied driving force was centered on oligomers of DP ≤4 under acidic conditions and sequentially spread to higher polymers as the pH increased. DP 6 to 8 COS is expected to be completely rejected by the NF membrane at a wider pH range (5.0 to 9.0). More important, the flexibility of COS was well conducted by the adjustment of pH. Nevertheless, in view of the objective of purification, a lower pH should be adopted for the impurity elimination. Interestingly, several small-sized peaks that were followed by octasaccharides were also characterized at 19.5 min (Figure 7). Due to the randomness of enzymatic hydrolysis on chitosan, this was probably attributed to the nonamers (DP 9 COS) existing in the syrup.
Figure 7

pH values vs. R obs of chitooligosaccharides at 16.0 bar and 40°C in NF process. The effects of pH ranged from 5.0 to 9.0 on rejections of glucosamine and DP 2 to 8 chitooligosaccharides were investigated. The Robs of chitooligosaccharides increased with pH, especially for the monomer, dimer, trimer, and tetramer. In addition, the flexibility of chitooligosaccharides was well conducted by pH.

3.7 Purification of DP 6 to 8 COS

Long-term experiments were carried out at 16.0 bar to enrich the DP 6 to 8 COS with a virgin concentration of 19.0 g/L (pH = 5.0, V0 = 16.0 L and T = 40°C). The performance of the NF membrane was evaluated by measuring the permeate flux and Robs of the target products as illustrated in Figures 8 and 9. In addition, the concentration ratio of DP 6 to 8 COS was monitored as a formula of V0/Vc. The flux value was about 102.4 L/(m2 h) at the beginning of the experiment, but it decreased to 30.2 L/(m2 h) when the concentration ratio reached to 6.0 (Figure 8). Then, the membrane was cleaned for 1 h. After that, the permeate flux of syrup was recovered to 53.5 L/(m2 h), which indicated that about 50% of virtual flux decline due to the increasing solid content and viscosity. However, the second drop of permeate flux was remarkable till the end of the run, as the value changed from 53.5 to 25.0 L/(m2 h) just 1.5 times of the later concentration. There was a direct reflection between the effect of solid contents and experimental records. A moderate concentration ratio and timely regenerations of the membrane should be arranged for acceptable efficiency in practice.
Figure 8

Concentration ratios vs. J v of 19.0 g/L chitooligosaccharide syrup. Long-term experiments were carried out at 16.0 bar for enrichment of DP 6 to 8 chitooligosaccharides. The flux was about 102.4 L/(m2 h) at the beginning, whereas it decreased heavily when the concentration rate was 6.0.
Figure 9

Concentration ratios vs. R obs of DP 6 to 8 chitooligosaccharides in the syrup. The Robs of DP 6 to 8 chitooligosaccharides went up when the circulating flux decreased. The phenomenon was accredited to the DSPM and steric hindrance pore (SHP) effects.

Moreover, the Robs of DP 6 to 8 COS went up when the circulating flux decreased (Figure 9). The result was principally accredited to the synergy with the DSPM and steric hindrance pore (SHP) effects. On the one hand, the anions preferred to be repelled while the cations were attracted to the NF membrane. The unique property transported the amino groups, which are commonly sensed in COS, to the permeate. Ultimately, the molecules containing NH4+ were separated from the syrup because of the electric attraction. On the other hand, the Robs of DP 6 to 8 COS was up to 1.0 after the concentration ratio increased to 8.0. The MWCO of the applied membrane is 500 Da, while the molecular weights of hexamer, heptamer, and octamer are 984, 1,145 and 1,306, respectively. There is a conspicuous difference in the sizes between membrane pores and DP 6 to 8 COS. Therefore, the observed retention behaviors illustrated that DP 6 to 8 COS were rejected sterically and a promising purity (82.2%) was eventually achieved via the NF purification designed.

3.8 MALDI-TOF-MS analysis of chitooligosaccharides

Matrix-assisted laser desorption/ionization time-of-flight (MALDI-TOF) is an outstanding tool for the comprehensive investigation of COS because the mass spectrum can exhibit the relative quantities of a mixture to be determined. Figure 9 shows the distribution of COS using MALDI-TOF-MS after NF enrichment. As expected, the final products were mainly composed of DP 6 to 8 COS, which was similar to the HPLC results mentioned before. In the spectrum, COS often contains intensive quasi-molecular ions, which is called [M + Na]+, because of its weak protonation degree. For instance, the peak at 1,007.1 m/z is attributed to the sodium form ([M + Na]+) of a hexa-oligomer (Figure 10).
Figure 10

MALDI-TOF mass spectrum of chitooligosaccharides. It showed the distribution of chitooligosaccharides. As expected, the final products were mainly composed of DP 6 to 8 chitooligosaccharides, which was similar with the HPLC results mentioned before.

4 Conclusions

In this study, the separation behavior of COS syrups, which were enriched by different concentrations of DP 6 to 8 COS, was investigated via a bench-scale NF process.

One negatively charged membrane with MWCO of 500 Da was selected to purify DP 6 to 8 COS. During the full recycle mode, the experimental results indicated that the retentions of these components increased with pressure before 16.0 bar. Also, the operation temperature was optimized. Although the circulating flux could be improved by elevating temperature, a greater wastage of DP 6 to 8 COS was irreversibly formed during the process as well. In addition, the effects of pH on Robs of COS were compared. The HPLC profiles illustrated that the Robs of COS within DP ≤4 in alkali conditions was significantly higher than that in acidic environment. This phenomenon could be explained by structural curling and sterical overlap due to hydrogen bonds. However, the mechanisms should be discussed in further researches.

Under the optimum conditions (TMP = 16.0 bar, T = 40°C, and pH = 5.0), the purification of DP 6 to 8 COS was carried out. It was found that the membrane could support a reluctant flux after the concentration ratio was over 6.0 in the syrup with the concentration of 19.0 g/L DP 6 to 8 COS. MALDI-TOF mass spectrum confirmed that DP 6 to 8 COS were dominant in the final products, and the purity was up to 82.2% (w/w) according to HPLC profiles. As a conclusion, the NF system equipped with a selected membrane module is a promising approach in the purification of DP 6 to 8 COS from specific syrups.



This work is financially supported by the National Natural Science Foundation of China (No. 31371725 and No. 31101381). Also, the authors are grateful to the Fundamental Research Funds for the Central Universities.

Authors’ Affiliations

State Key Laboratory of Bioreactor Engineering, R&D Center of Separation and Extraction Technology in Fermentation Industry, East China University of Science and Technology
Shanghai Collaborative Innovation Center for Biomanufacturing Technology


  1. Xia W, Liu P, Zhang J, Chen J: Biological activities of chitosan and chitooligosaccharides. Food Hydrocolloids 2011, 25: 170–179. 10.1016/j.foodhyd.2010.03.003View ArticleGoogle Scholar
  2. Kim S, Rajapakse N: Enzymatic production and biological activities of chitosan oligosaccharides (COS): a review. Carbohydr Polym 2005, 62: 357–368. 10.1016/j.carbpol.2005.08.012View ArticleGoogle Scholar
  3. Benhabiles MS, Salah R, Lounici H, Drouiche N, Goosen MFA, Mameri N: Antibacterial activity of chitin, chitosan and its oligomers prepared from shrimp shell waste. Food Hydrocolloids 2012, 29: 48–56. 10.1016/j.foodhyd.2012.02.013View ArticleGoogle Scholar
  4. Huang RH, Du YM, Yang JH, Fan L: Influence of functional groups on the in vitro anticoagulant activity of chitosan sulfate. Carbohy Res 2003, 338: 483–489. 10.1016/S0008-6215(02)00505-0View ArticleGoogle Scholar
  5. Lin S, Lin Y, Chen H: Low molecular weight chitosan prepared with the aid of cellulase, lysozyme and chitinase: characterisation and antibacterial activity. Food Chem 2009, 116: 47–53. 10.1016/j.foodchem.2009.02.002View ArticleGoogle Scholar
  6. Kim KW, Thomas RL: Antioxidative activity of chitosans with varying molecular weights. Food Chem 2007, 101: 308–313. 10.1016/j.foodchem.2006.01.038View ArticleGoogle Scholar
  7. Zhang Y, Huo M, Zhou J, Yu D, Wu Y: Potential of amphiphilically modified low molecular weight chitosan as a novel carrier for hydrophobic anticancer drug: synthesis, characterization, micellization and cytotoxicity evaluation. Carbohydr Polym 2009, 77: 231–238. 10.1016/j.carbpol.2008.12.034View ArticleGoogle Scholar
  8. Zhang J, Zhang W, Mamadouba B, Xia W: A comparative study on hypolipidemic activities of high and low molecular weight chitosan in rats. Int J Biol Macromol 2012, 51: 504–508. 10.1016/j.ijbiomac.2012.06.018View ArticleGoogle Scholar
  9. Chang Y, Chang C, Huang T, Chen S, Lee J, Chung Y: Effects of low molecular weight chitosans on aristolochic acid-induced renal lesions in mice. Food Chem 2011, 129: 1751–1758. 10.1016/j.foodchem.2011.06.044View ArticleGoogle Scholar
  10. Berth G, Dautzenberg H: The degree of acetylation of chitosans and its effect on the chain conformation in aqueous solution. Carbohydr Polym 2002, 47: 39–51. 10.1016/S0144-8617(00)00343-XView ArticleGoogle Scholar
  11. Lee EH, Lee JJ, Jon SY: A novel approach to oral delivery of insulin by conjugating with low molecular weight chitosan. Bioconjugate Chem 2010, 21: 1720–1723. 10.1021/bc100093vView ArticleGoogle Scholar
  12. Li N, Wang CY, Wang M, Sun X, Nie S, Pan W: Liposome coated with low molecular weight chitosan and its potential use in ocular drug delivery. Int J Pharm 2009, 379: 131–138. 10.1016/j.ijpharm.2009.06.020View ArticleGoogle Scholar
  13. Chien PJ, Sheu F, Lin HR: Coating citrus (Murcott tangor) fruit with low molecular weight chitosan increases postharvest quality and shelf life. Food Chem 2007, 100: 1160–1164. 10.1016/j.foodchem.2005.10.068View ArticleGoogle Scholar
  14. Abd–Elmohdy FA, Sayed ZE, Essam S, Hebeish A: Controlling chitosan molecular weight via bio-chitosanolysis. Carbohydr Polym 2010, 82: 539–542. 10.1016/j.carbpol.2010.02.051View ArticleGoogle Scholar
  15. Jeon Y, Kim S: Production of chitooligosaccharides using an ultrafiltration membrane reactor and their antibacterial activity. Carbohydr Polym 2000, 41: 133–141. 10.1016/S0144-8617(99)00084-3View ArticleGoogle Scholar
  16. Fan W, Yan W, Xu Z, Ni H: Formation mechanism of monodisperse, low molecular weight chitosan nanoparticles by ionic gelation technique. Colloids Surf B 2012, 90: 21–27. 10.1016/j.colsurfb.2011.09.042View ArticleGoogle Scholar
  17. Cabrera JC, Custem PV: Preparation of chitooligosaccharides with degree of polymerization higher than 6 by acid or enzymatic degradation of chitosan. Biochem Eng J 2005, 25: 165–172. 10.1016/j.bej.2005.04.025View ArticleGoogle Scholar
  18. Simonnot MO, Castel C, Nicolai M, Rosin C, Sardin M, Jauffret H: Boron removal from drinking water with a boron selective resin: is the treatment really selective. Water Res 2000, 34: 109–116. 10.1016/S0043-1354(99)00130-XView ArticleGoogle Scholar
  19. Nadav N: Boron removal from seawater reverse osmosis permeate utilizing selective ion exchange resin. Desalination 1999, 124: 131–135. 10.1016/S0011-9164(99)00097-1View ArticleGoogle Scholar
  20. Han YP, Lin Q, He XW: Research on desalination and purification characteristics of chitobiose solution with nanofiltration membrane. Membrane Science and Technology 2009, 29: 105–109.Google Scholar
  21. Han YP, Lin Q, Wang XL: Feasibility study on chitooligosaccharides purification by nanofiltration membranes. Ion Exchange and Adsorption 2012, 28: 86–96.Google Scholar
  22. Xu W, Jiang C, Kong X, Liang Y, Rong M, Liu W: Chitooligosaccharides and N-acetyl-D-glucosamine stimulate peripheral blood mononuclear cell-mediated antitumor immune response. Mol Med Rep 2012, 6: 385–390.Google Scholar
  23. Zhao HF, Hua X, Yang RJ, Zhao LM, Zhao W, Zhang Z: Diafiltration process on xylo-oligosaccharides syrup using nanofiltration and its modeling. Int J Food Sci Tech 2012, 47: 32–39. 10.1111/j.1365-2621.2011.02803.xView ArticleGoogle Scholar
  24. Zhang Z, Yang RJ, Zhang S, Zhao H, Hua X: Purification of lactose syrup by using nanofiltration in a diafiltration mode. J Food Eng 2011, 105: 112–118. 10.1016/j.jfoodeng.2011.02.013View ArticleGoogle Scholar
  25. Bowen WR, Mohammad AW: Diafiltration by nanofiltration: prediction and optimization. AIChE J 1998, 44: 1799–1812. 10.1002/aic.690440811View ArticleGoogle Scholar


© Dong et al.; licensee Springer. 2014

This article is published under license to BioMed Central Ltd. This is an Open Access article distributed under the terms of the Creative Commons Attribution License (, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly credited.