Methods for enzymatic production of glucosamine salts and the purification methods thereof

Abstract

Disclosed in the present disclosure are methods for enzymatic production of glucosamine salts and the purification methods thereof, and belongs to the technical field of biological engineering. In the present disclosure, liquid containing N-acetylglucosamine is used as a raw material, subjected to hydrolysis with deacetylase to obtain glucosamine and acetic acid, and followed by elution on a cation exchange column with an acidic eluent and separation to obtain the glucosamine salt. Meanwhile, a by-product, namely sodium acetate, is recovered by anion exchange. The obtained glucosamine salt is subjected to concentration, crystallization, decolorization, and drying to obtain a high-purity glucosamine salt crystal. According to the present disclosure, processes for recycling of an enzyme, a residual substrate, and acetic acid are combined. Moreover, the loss rate of resin is low under operation conditions at room temperature, and the production of a hydrochloric acid waste liquid is extremely low.

Claims

1. A method for enzymatic production of a glucosamine salt and a purification method therefor, comprising: subjecting a solution containing N-acetylglucosamine as a raw material to catalytic hydrolysis with deacetylase or a preparation containing deacetylase to obtain an enzymatic hydrolysis product; subjecting the enzymatic hydrolysis product to filtration with a membrane, recovering the deacetylase from an obtained membrane retentate, recycling the deacetylase for the catalytic hydrolysis, and using an obtained membrane dialysate in cation exchange treatment; subjecting the enzymatic hydrolysis product or the membrane dialysate to cation exchange and elution with an acidic eluent to obtain a glucosamine salt; and subjecting a positive column effluent obtained in the cation exchange process to anion exchange and elution with an alkaline eluent to recover acetate, and subjecting a negative column effluent obtained in the anion exchange process to concentration and circular sending back to the catalytic hydrolysis process involving the deacetylase.

2. The method according to claim 1, wherein the membrane is a membrane assembly prepared from a ceramic material or a membrane assembly prepared from an organic material; an ultrafiltration membrane has a molecular weight cut-off of 5-200 kDa; a resin for the cation exchange comprises a cation exchange resin with a sulfonyl group; a resin for the anion exchange comprises an anion exchange resin with a quaternary ammonium group; and a device for the cation exchange and/or the anion exchange is a fixed bed for ion exchange, a continuous moving bed for ion exchange, or a simulated moving bed for ion exchange.

3. The method according to claim 1, wherein the acidic eluent is hydrochloric acid, sulfuric acid, phosphoric acid, pyruvic acid, or citric acid with a concentration of 0.3-4.0 mol/L.

4. The method according to claim 1, wherein the alkaline eluent is a NaOH solution or a KOH solution with a concentration of 0.30-3.0 mol/L.

5. The method according to claim 1, wherein in the ion exchange process, adsorption or elution is conducted at a temperature of 20-75° C. and a feeding flow rate of 2.0-10.0 BV/h; and the eluent has a flow rate of 1.0-8.0 BV/h.

6. The method according to claim 5, wherein the obtained glucosamine salt is subjected to concentration, crystallization, and drying to obtain a high-purity glucosamine salt.

7. The method according to claim 6, wherein the concentration is evaporation concentration; the evaporation concentration is single-effect evaporation concentration or multiple-effect evaporation concentration, and a last-effect evaporator has a vacuum degree of 80-98 kPa; the crystallization is conducted at a temperature of 5-40° C.; the drying is low-temperature vacuum drying or flash drying; the low-temperature vacuum drying is conducted at a temperature of 40-80° C. and a vacuum degree of 70-95 kPa; and the flash drying is conducted at a hot air temperature of 120-300° C.

8. The method according to claim 7, wherein the method further comprises decolorization of a mother liquor; a decolorization method is adsorption decolorization with activated carbon; and a decolorized mother liquor is recycled in a concentration process.

9. The method according to claim 8, wherein according to the decolorization method, the consumption of the activated carbon is 0.01-2% (w/v) of that of a raw material solution; and the activated carbon is a carbon rod, a carbon column, or granular activated carbon.

10. The method according to claim 1, comprising the following steps: (1) using an N-acetylglucosamine solution with a concentration of 40-150 g/L as a raw material, adding the preparation containing deacetylase, and carrying out an enzymatic reaction under stirring in a pH range of 4-8 at a temperature of 25-55° C. for 10-90 minutes; (2) subjecting an enzymatic hydrolysis product obtained after the reaction in step (1) to filtration with an ultrafiltration membrane or a nanofiltration membrane to obtain an ultrafiltration membrane dialysate containing glucosamine and a membrane concentrate, and recycling an enzyme solution of the membrane concentrate to participate in a next batch of enzymatic reaction in step (1); (3) subjecting the ultrafiltration membrane dialysate obtained in step (2) to adsorption with a cation exchange resin, subjecting the cation exchange resin to continuous elution with the acidic eluent to obtain an eluate containing a glucosamine salt, and washing out the cation exchange resin with deionized water to obtain the positive column effluent containing N-acetylglucosamine and acetic acid; (4) subjecting the positive column effluent flowing through the cation exchange resin in step (3) to adsorption with an anion exchange resin, and subjecting the anion adsorption resin to elution with the alkaline eluent to separate an eluate containing acetate; and (5) recycling the negative column effluent flowing through the anion exchange resin in step (4) to participate in a next batch of enzymatic reaction process in step (1), or subjecting the negative column effluent flowing through the anion exchange resin in step (4) to concentration first, followed by recycling to participate in a next enzymatic reaction process in step (1), wherein a concentration method is vacuum concentration, concentration by filtration with a nanofiltration membrane or a reverse osmosis membrane, or multiple-effect evaporation concentration.

11. The method according to claim 10, wherein in step (5), the nanofiltration membrane is a ceramic membrane with a pore size of 0.5-2 nm; and the reverse osmosis membrane is an organic spiral-wound membrane or a ceramic membrane.

12. The method according to claim 10, wherein the eluate containing the glucosamine salt obtained in step (3) is directly transported to a spray drying device at a feeding flow rate of 5 m.sup.3/h, and spray drying is conducted at an inlet air temperature of 150° C.

Description

BRIEF DESCRIPTION OF FIGURES

[0048] FIG. 1 shows an extraction process route of a glucosamine salt.

DETAILED DESCRIPTION

Technical Terms

[0049] A glucosamine salt refers to a glucosamine salt product obtained after elution on a cation exchange column with different acids, including but not limited to any one of a glucosamine hydrochloride, a glucosamine sulfate, a glucosamine phosphate, a glucosamine pyruvate, and a glucosamine citrate.

[0050] A membrane dialysate refers to a liquid flowing through a membrane material during filtration with a membrane.

[0051] A membrane concentrate refers to a liquid that cannot flow through a membrane material and is retained during filtration with a membrane.

[0052] An eluate refers to a liquid obtained after an eluent (such as an acidic solution or an alkaline solution) flows through a saturated ion exchange resin during ion exchange.

[0053] A column effluent refers to a liquid that is not adsorbed by an ion exchange resin, directly flows out from a raw material solution and is washed out by deionized water during ion exchange chromatography.

[0054] The activity unit of deacetylase is defined as 1 U=1 mmol/min, and that is to say, 1 mmol of glucosamine obtained after a reaction for 1 minute is defined as 1 U enzyme activity unit.

[0055] The purification and recovery rate of a glucosamine salt is as follows: since an enzymatic reaction, ion exchange, and other units are involved in a method for enzymatic production of the glucosamine salt and a purification process therefor, the molecular structure of a reactant is changed. The recovery rate is calculated based on the mass of glucosamine.

[0056] The glucosamine salt and N-acetylglucosamine are quantified by an HPLC analysis method. An Agilent 1260 series is used as a liquid chromatograph. A Thermo ODS-2 Hypersil C18 column (250 mm×4.0 mm) is used as a chromatographic column. A glucosamine salt sample to be tested is filtered with a 0.22 μm microfiltration membrane, and then injected into the chromatographic column at an injection volume of 10 μl. The N-acetylglucosamine and acetic acid are analyzed by an HPX-87H column (Bio-Rad, USA) as a chromatographic column. A differential refractometer detector is used. 5 mmol/L H.sub.2SO.sub.4 is used as a mobile phase, and detection is carried out at a flow rate of 0.6 ml/min and a temperature of 40° C.

Example 1

[0057] According to the process route as shown in FIG. 1, operation steps are as follows.

[0058] (1) An N-acetylglucosamine solution with a concentration of 40-150 g/L was used as a raw material, a deacetylase solution or a deacetylase preparation was added in a proportion of 10-30 U/g of N-acetylglucosamine, and an enzymatic reaction was carried out under stirring in a pH range of 4.0-8.0 at a temperature of 25-45° C. for 10-40 minutes. The deacetylase preparation was selected from commercial enzymes capable of removing acetyl in N-acetylglucosamine by hydrolysis. In the step, the acetyl in an N-acetylglucosamine molecule was removed specifically. An enzymatic hydrolysis product including glucosamine and acetic acid as main components was obtained after the reaction. The enzymatic reaction was preferably carried out at a pH of 7.0-8.0.

[0059] (2) The enzymatic hydrolysis product obtained after the reaction in step (1) was transported to an ultrafiltration membrane device. The ultrafiltration membrane had a molecular weight cut-off of 5-200 kDa, preferably 5-30 kDa. A membrane concentrate was subjected to dialysis with water, and an ultrafiltration membrane dialysate containing glucosamine and a membrane concentrate containing deacetylase were separately collected. After dialysis with a membrane was completed, the recovery rate of the deacetylase was 80-90%.

[0060] (3) An enzyme solution obtained after concentration with the membrane in step (2) was sent back to a deacetylase solution storage tank to participate in a next batch of enzymatic reaction process.

[0061] The ultrafiltration membrane dialysate containing glucosamine obtained in step (2) was continuously pumped into a positive column filled with an acidic resin (such as a cation exchange resin with a sulfonyl group) of a simulated moving bed at a feeding flow rate of 2.0-10.0 BV/h to make the glucosamine in the dialysate adsorbed to the positive column.

[0062] The positive column was washed out with deionized water to obtain a positive column effluent containing N-acetylglucosamine and acetic acid.

[0063] The positive column was subjected to continuous elution with hydrochloric acid, sulfuric acid, phosphoric acid, pyruvic acid, citric acid, and other acidic eluents with a concentration of 0.30-3.0 mol/L at a temperature of 20-70° C., preferably 25° C., to obtain a eluate containing a corresponding glucosamine salt.

Example 2

[0064] According to the process route as shown in FIG. 1, operation steps are as follows.

[0065] (1) An N-acetylglucosamine solution with a concentration of 40-150 g/L was used as a raw material, a deacetylase solution or a deacetylase preparation was added in a proportion of 10-30 U/g of N-acetylglucosamine, and an enzymatic reaction was carried out under stirring in a pH range of 4.0-8.0 at a temperature of 25-45° C. for 10-40 minutes. The deacetylase preparation was selected from commercial enzymes capable of removing acetyl in N-acetylglucosamine by hydrolysis. In the step, the acetyl in an N-acetylglucosamine molecule was removed specifically. An enzymatic hydrolysis product including glucosamine and acetic acid as main components was obtained after the reaction. The enzymatic reaction was preferably carried out at a pH of 7.0-8.0.

[0066] (2) The enzymatic hydrolysis product obtained after the reaction in step (1) was transported to an ultrafiltration membrane device. The ultrafiltration membrane had a molecular weight cut-off of 5-200 kDa, preferably 5-30 kDa. A membrane concentrate was subjected to dialysis with water, and an ultrafiltration membrane dialysate containing glucosamine and a membrane concentrate containing deacetylase were separately collected. After dialysis with a membrane was completed, the recovery rate of the deacetylase was 80-90%.

[0067] (3) An enzyme solution obtained after concentration with the membrane in step (2) was sent back to a deacetylase solution storage tank to participate in a next batch of enzymatic reaction process.

[0068] The ultrafiltration membrane dialysate containing glucosamine obtained in step (2) was continuously pumped into a positive column filled with an acidic resin (such as a cation exchange resin with a sulfonyl group) of a simulated moving bed at a feeding flow rate of 2.0-10.0 BV/h to make the glucosamine in the dialysate adsorbed to the positive column.

[0069] The positive column was washed out with deionized water to obtain a positive column effluent containing N-acetylglucosamine and acetic acid.

[0070] The positive column was subjected to continuous elution with hydrochloric acid, sulfuric acid, phosphoric acid, pyruvic acid, citric acid, and other acidic eluents with a concentration of 0.30-3.0 mol/L at a temperature of 20-70° C., preferably 25° C., to obtain a eluate containing a corresponding glucosamine salt, which was used in subsequent processes of concentration, crystallization, and drying.

[0071] (4) The positive column effluent in step (3) was further transported to a negative column filled with an alkaline anion exchange resin (such as an anion exchange resin with a quaternary ammonium salt) at a feeding flow rate of 2.0-10.0 BV/h. Adsorption and elution were conducted at a temperature of 20-65° C., preferably 25° C., to make the acetic acid adsorbed to the negative column.

[0072] The negative column was washed out with deionized water to obtain a negative column effluent containing N-acetylglucosamine.

[0073] The negative column was subjected to continuous elution with NaOH or KOH and other alkaline eluents with a concentration of 0.30-3.0 mol/L at a rate of 1.0-8.0 BV/h to separate a eluate rich in acetate. The eluate was transported to a sewage treatment workshop to serve as a supplementary carbon source for nitrogen and phosphorus removal processes, and was also used as a chemical raw material.

[0074] (5) The negative column effluent flowing through the negative column in step (4) was transported to a nanofiltration membrane concentration device or a reverse osmosis membrane concentration device.

[0075] The nanofiltration membrane was a ceramic membrane with a pore size of 0.5-2 nm and an operation pressure of 2-5 atm.

[0076] The reverse osmosis membrane was an organic spiral-wound membrane or a ceramic membrane with a molecular weight cut-off of 50-100 Da and an operation pressure of 4-10 atm.

[0077] The N-acetylglucosamine obtained after concentration with the membrane had a final concentration of 10-15% (w/v). A membrane concentrate was recycled to an N-acetylglucosamine storage tank to participate in a next batch of enzymatic reaction process in step (1).

[0078] (6) The eluate of the positive column in step (3) was pumped into a multiple-effect evaporator for evaporation concentration. The multiple-effect evaporation concentration was triple-effect evaporation at gradient temperature. For example, the first-effect evaporator, the second-effect evaporator and the third-effect evaporator had a temperature of 80° C., 70° C. and 60° C. respectively, and the third-effect evaporator had a vacuum degree of 80-98 kPa.

[0079] (7) An effluent obtained after the concentration by the multiple-effect evaporator in step (6) flowed into a crystallizer. The crystallization temperature was controlled at 5-40° C. by controlling the temperature of a jacket of the crystallizer. A crystal suspension generated by the crystallizer was sent to a solid-liquid separation device for separation to obtain a mother liquor and a glucosamine salt crystal mud separately. A centrifuge with a continuous centrifugal function or a horizontal scraper discharge centrifuge was selected as the separation device.

[0080] (8) The mother liquor obtained after the separation in step (7) was subjected to decolorization with activated carbon. After the decolorization was completed, the mother liquor was sent back to the multiple-effect evaporator in step (6). The glucosamine salt crystal mud was transported to a drying device to obtain a dried glucosamine salt crystal. The recovery rate of the concentration, crystallization and drying units can reach 98%.

Example 3

[0081] According to the process route as shown in FIG. 1, operation steps are as follows.

[0082] (1) 350 m.sup.3 of an N-acetylglucosamine solution with a concentration of 102 kg/m.sup.3 was collected in a storage tank and pumped into an enzymatic reaction tank, a deacetylase solution was added in a proportion of 10-25 U/g of N-acetylglucosamine, and an enzymatic reaction was carried out under stirring at a pH of 7.0-8.0 and a temperature of 37° C. for 30 minutes.

[0083] (2) An enzymatic hydrolysis product obtained after the reaction in step (1) was pumped into an ultrafiltration membrane device. The ultrafiltration membrane had a molecular weight cut-off of 5,000 Da. 60 m.sup.3 of pure water was added for dialysis of a membrane concentrate, and an ultrafiltration membrane dialysate and a membrane concentrate were separately collected. A glucosamine dialysate with a total content of 380 m.sup.3 and a concentration of 56.3 kg/m.sup.3 was collected. 30 m.sup.3 of an enzyme solution of the membrane concentrate was sent back to a deacetylase solution storage tank to participate in a next batch of enzymatic reaction process.

[0084] (3) The glucosamine dialysate obtained in step (2) was continuously pumped into a positive column filled with a 001×7 strongly acidic styrene resin of a simulated moving bed at a feeding flow rate of 4.0 BV/h. Feeding and elution were conducted at a temperature of 25° C. The glucosamine in the dialysate was adsorbed to the positive column. The positive column was washed out with deionized water to obtain a positive column effluent containing a neutral sugar and acetic acid.

[0085] The positive column was subjected to continuous elution with a hydrochloric acid solution with a concentration of 2 mol/L at a flow rate of 3.0 BV/h to obtain 91.7 m.sup.3 of a eluate containing a glucosamine hydrochloride with a concentration of 252 kg/m.sup.3.

[0086] (4) The positive column effluent in step (3) was further transported to a negative column filled with an anion exchange resin of the simulated moving bed at a flow rate of 4.0 BV/h. The negative column was washed out with deionized water to obtain a negative column effluent containing N-acetylglucosamine with a concentration of about 3%.

[0087] The negative column was subjected to continuous elution with a NaOH solution with a concentration of 1.5 mol/L to separate 80.6 m.sup.3 of an eluate rich in sodium acetate (107.5 kg/m.sup.3). The negative column was filled with a 201×7 strongly alkaline styrene resin.

[0088] (5) 514.6 m.sup.3 of the column effluent flowing through the negative column in step (4) was transported to a nanofiltration membrane concentration device. The nanofiltration membrane had a pore size of 1 nm and an operation pressure of 0.5-1.0 atm. A nanofiltration membrane concentrate containing N-acetylglucosamine with a total content of 89.3 m.sup.3 and a concentration of 125 g/L was obtained after concentration. The nanofiltration membrane concentrate was recycled to an N-acetylglucosamine storage tank to participate in a next batch of enzymatic reaction process.

[0089] In the first reaction and purification process, 23.1 tons of a glucosamine hydrochloride can be obtained, and the recovery rate of the glucosamine hydrochloride reaches 66.2%.

[0090] After the second circular reaction that 89.3 m.sup.3 of the concentrate obtained after concentration with the nanofiltration membrane was circulated to the N-acetylglucosamine solution storage tank and the enzyme solution of the membrane concentrate in step (2) was sent back to the enzymatic reaction tank, a glucosamine hydrochloride solution with a content of 45 m.sup.3 and a concentration of 238 kg/m.sup.3 can be recovered, and the total recovery rate of the glucosamine hydrochloride reaches 97%.

[0091] To continue the above process, eluents of the glucosamine hydrochloride obtained in step (3) in the first batch reaction and the second batch reaction were combined, and then subjected to concentration, crystallization, and drying. Details are as follows.

[0092] (6) A combined solution containing the glucosamine hydrochloride was pumped into a triple-effect evaporator at a feeding flow rate of 6 m.sup.3/h. A last-effect evaporator had a vacuum degree of 90 kPa. Cooling water had an inlet water temperature of 8-15° C., and a discharged product had a concentration of 720 g/L.

[0093] (7) An effluent of the triple-effect evaporator flowed into a crystallizer. The crystallization temperature was controlled at 40° C. by controlling the temperature of a jacket of the crystallizer. A crystal suspension produced by the crystallizer was sent to a horizontal scraper discharge centrifuge for separation to obtain a mother liquor and a glucosamine hydrochloride crystal mud separately.

[0094] (8) The mother liquor was sent to an activated carbon decolorization column at a flow rate of 0.5 m.sup.3/h for decolorization. After the decolorization was completed, the mother liquor was sent to the storage tank in front of the triple-effect evaporator. The glucosamine hydrochloride crystal mud separated by the horizontal scraper discharge centrifuge was sent to a flash dryer through a screw conveyor for flash drying at an inlet air temperature of 150° C. and an outlet air temperature of 80° C. to obtain a glucosamine hydrochloride crystal.

[0095] The total recovery rate of the concentration, crystallization and drying units in steps (6)-(8) can reach 98%.

[0096] In the whole production process, when 1 ton of the glucosamine hydrochloride is produced, 500 kg of a concentrated hydrochloric acid solution, 550 L of a 30% NaOH solution and 10 tons of pure water are consumed, 9.7 tons of wastewater is produced, and about 10 kg of the cation exchange resin and the anion exchange resin are separately consumed.

Example 4

[0097] According to the process route as shown in FIG. 1, the difference is that on the basis of Example 3, a nanofiltration membrane concentration device was replaced with a reverse osmosis ceramic membrane device, and that is to say, a negative column effluent obtained in step (4) was collected into the reverse osmosis ceramic membrane device. The reverse osmosis membrane had a pore size of 1 nm and an operation pressure of 0.5-1.0 MPa. A liquid obtained after concentration by the reverse osmosis ceramic membrane device was sent back to an enzymatic reaction tank to participate in a next batch of enzymatic reaction process.

[0098] In the production process, when 1 ton of a glucosamine hydrochloride is produced, 11 tons of pure water is consumed, and 10.5 tons of wastewater is produced.

Example 5

[0099] According to the process route as shown in FIG. 1, the difference is that on the basis of Example 3, a hydrochloric acid solution in step (3) was replaced with a sulfuric acid solution, and that is to say, in step (3), glucosamine adsorbed to a positive column was subjected to elution with 1 mol/L of the sulfuric acid solution to obtain a product, namely a glucosamine sulfate.

Example 6

[0100] According to the process route as shown in FIG. 1, the difference is that on the basis of Example 3, a hydrochloric acid solution in step (3) was replaced with a phosphoric acid solution, and that is to say, in step (3), glucosamine adsorbed to a positive column was subjected to elution with 1 mol/L of the phosphoric acid solution to obtain a product, namely a glucosamine phosphate.

Example 7

[0101] According to the process route as shown in FIG. 1, the difference is that on the basis of Example 3, a hydrochloric acid solution in step (3) was replaced with a citric acid solution, and that is to say, in step (3), glucosamine adsorbed to a positive column was subjected to elution with 1 mol/L of the citric acid solution to obtain a product, namely a glucosamine citrate.

Example 8

[0102] According to the process route as shown in FIG. 1, the difference is that on the basis of Example 3, a hydrochloric acid solution in step (3) was replaced with a pyruvic acid solution, and that is to say, in step (3), glucosamine adsorbed to a positive column was subjected to elution with 2 mol/L of the pyruvic acid solution to obtain a product, namely a glucosamine pyruvate.

Example 9

[0103] According to the process route as shown in FIG. 1, the difference is that on the basis of Example 3, a simulated moving bed in step (3) was replaced with a continuous moving bed device. A positive column and a negative column were filled with unchanged resins. The positive column was filled with a 001×7 strongly acidic styrene cation exchange resin, and the negative column was filled with a 201×7 strongly alkaline styrene anion exchange resin. When 1 ton of a product is produced, 16 kg of the cation exchange resin, 14 kg of the anion exchange resin, 600 kg of concentrated hydrochloric acid and 650 L of a 30% sodium hydroxide solution are consumed, and 15 tons of wastewater is produced.

Example 10

[0104] According to the process route as shown in FIG. 1, the differences are that on the basis of Example 3, a simulated moving bed in step (3) was replaced with a fixed bed ion exchange device, a positive column was filled with a 201×7 strongly alkaline styrene anion exchange resin, and a negative column was filled with a 001×7 strongly acidic styrene cation exchange resin. When 1 ton of a product is produced, 30 kg of the cation exchange resin, 28 kg of the anion exchange resin, 1,300 kg of concentrated hydrochloric acid and 1,400 L of a 30% sodium hydroxide solution are consumed, and 50 tons of wastewater is produced.

Example 11

[0105] According to the process route as shown in FIG. 1, the differences are that on the basis of Example 5, triple-effect evaporation concentration and crystallization were omitted, an eluate rich in a glucosamine sulfate obtained after elution in a positive column of a simulated moving bed was directly transported to a spray drying device at a feeding flow rate of 5 m.sup.3/h, and spray drying was conducted at an inlet air temperature of 150° C. After the drying was completed, 41.5 tons of a glucosamine sulfate powder was obtained. The purity of the product reaches 99%.

Example 12

[0106] According to the process route as shown in FIG. 1, the differences are that on the basis of Example 3, an enzymatic reaction solution obtained in step (1) was continuously pumped into a positive column in step (3) at a feeding flow rate of 3.0 BV/h, feeding and elution were conducted at a temperature of 30° C., subsequent steps were the same as those in Example 2, and a product, namely a glucosamine hydrochloride, was obtained.

Comparative Example 1

[0107] With reference to a method for separating a D-glucosamine hydrochloride in a patent application with an application number of CN2016112278411, 50 m.sup.3 of an N-acetylglucosamine solution with a concentration of 102 kg/m.sup.3 in a storage tank was collected, steam was introduced to heat the solution to 95° C., and the solution was pumped into an exchange column filled with a strongly acidic cation exchange resin at a temperature of 90° C. to make the N-acetylglucosamine undergo a reaction with the cation exchange resin for 240 minutes. After the reaction was completed, pure water was introduced to wash the cation exchange resin, and 40 m.sup.3 of a column effluent containing acetic acid was collected. After the washing was completed, 12% of hydrochloric acid was introduced to conduct elution on the cation exchange column, where the elution was conducted at a flow rate of 1.5 BV/h. 42 m.sup.3 of a eluate containing a glucosamine hydrochloride with a concentration of 103 kg/m.sup.3 was collected, and the recovery rate of this step was 88.6%. 0.2% (w/v) of activated carbon was added into the eluate for decolorization, and then the solution was pumped into a triple-effect evaporation concentrator, followed by crystallization, centrifugation, and drying to obtain 4,410 kg of a glucosamine hydrochloride with a total recovery rate of 80.2%. Since the reaction of the N-acetylglucosamine and the cation exchange resin is carried out at high temperature for a long time, a pigment is likely to be produced in the reaction process, and the loss of the ion exchange resin is increased. When a ton of the glucosamine hydrochloride is produced, 1,100 kg of concentrated hydrochloric acid and 120 kg of the cation exchange resin are consumed, 30 m.sup.3 of wastewater with a high content of an inorganic acid and high COD is produced, and the acetic acid cannot be recovered in the production process.

TABLE-US-00001 TABLE 1 Extraction effects of a glucosamine salt with different cation exchange modes Use amount of a concentrated hydrochloric Production of Cation Loss of resin acid solution wastewater Product Case exchange (kg/ton of (kg/ton of (m.sup.3/ton of recovery rate number mode product) product) product) (%) Example 3 Simulated 20 500 9.7 99 moving bed Example 9 Continuous 30 600 15 99 moving bed Example 10 Fixed bed 58 1,300 50 95 Comparative Deacetylation 120 1,100 30 87.4 Example 1 reaction coupled with cation exchange resin adsorption

[0108] The inventor has also tried to adjust process parameters of enzymatic hydrolysis, separation and purification to achieve the effects that within the range of the preferred parameters in Example 1, the product recovery rate of the ion exchange unit can reach 99%, the loss of the filling material is controlled within the range of 20 kg/ton, the use amount of the acidic solution is controlled within the range of 600 kg/ton of product, and the production of the wastewater is less than 10 m.sup.3/ton of product.

Comparative Example 2

[0109] With reference to a method disclosed in CN2013106719979, the differences are that a raw material, namely a glucosamine hydrochloride mother liquor, was replaced with an enzymatic reaction solution containing glucosamine, and the operation step of transferring a eluate of a cation exchange column to an anion exchange column was omitted. A total of 50 m.sup.3 of a deacetylase reaction solution and a membrane dialysate (containing glucosamine and acetic acid) obtained after dialysis with an ultrafiltration membrane were collected in a storage tank. An N-acetylglucosamine solution with a concentration of 89 kg/m.sup.3 was pumped into an exchange column filled with a strongly acidic cation exchange resin at a temperature of 32° C. to make the N-acetylglucosamine adsorbed to the cation exchange resin. Pure water was introduced to wash out the cation exchange resin, and a total of 60 m.sup.3 of a column effluent containing acetic acid was collected. After the washing was completed, 0.3 mol/L of a hydrochloric acid solution was introduced to conduct elution on the cation exchange column, where the elution was conducted at a flow rate of 1.5 BV/h. 31 m.sup.3 of a glucosamine hydrochloride solution with a concentration of 126 kg/m.sup.3 was collected, and the recovery rate was 87.8%. A eluate was heated to 60° C., 1% of powdered activated carbon was added for decolorization, and after filtration was completed, 30.5 m.sup.3 of a glucosamine hydrochloride solution containing a filtrate with a concentration of 125 kg/m.sup.3 was obtained. Then, the solution was pumped into a triple-effect evaporation concentrator, followed by crystallization, centrifugation, and drying to obtain 3,585 kg of a light yellow glucosamine hydrochloride crystal with a total recovery rate of 80.6%. According to the method, since the decolorization and concentration are conducted in sequence, the consumption of the activated carbon is high. When a ton of the glucosamine hydrochloride is produced, 900 kg of concentrated hydrochloric acid and 20 kg of the cation exchange resin are consumed, and 30 m.sup.3 of wastewater with high COD is produced.

[0110] Although the present disclosure has been disclosed as preferred examples described above, the preferred examples are not intended to limit the present disclosure. Various changes and modifications can be made by any person familiar with the art without departing from the spirit and scope of the present disclosure. Therefore, the protection scope of the present disclosure shall be as defined by the claims.