CN103483395A - Method and system for purifying trehalose from mixture containing trehalose and impurity saccharide - Google Patents
Method and system for purifying trehalose from mixture containing trehalose and impurity saccharide Download PDFInfo
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- CN103483395A CN103483395A CN201310412037.0A CN201310412037A CN103483395A CN 103483395 A CN103483395 A CN 103483395A CN 201310412037 A CN201310412037 A CN 201310412037A CN 103483395 A CN103483395 A CN 103483395A
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- trehalose
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- HDTRYLNUVZCQOY-WSWWMNSNSA-N Trehalose Natural products O[C@@H]1[C@@H](O)[C@@H](O)[C@@H](CO)O[C@@H]1O[C@@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 HDTRYLNUVZCQOY-WSWWMNSNSA-N 0.000 title claims abstract description 83
- HDTRYLNUVZCQOY-LIZSDCNHSA-N Trehalose Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@@H]1O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 HDTRYLNUVZCQOY-LIZSDCNHSA-N 0.000 title claims abstract description 81
- 239000000203 mixture Substances 0.000 title claims abstract description 42
- 150000001720 carbohydrates Chemical class 0.000 title claims abstract description 9
- 239000012535 impurity Substances 0.000 title abstract 4
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 44
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 24
- UFHFLCQGNIYNRP-UHFFFAOYSA-N hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 19
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 14
- GUBGYTABKSRVRQ-YOLKTULGSA-N Maltose Natural products O([C@@H]1[C@H](O)[C@@H](O)[C@H](O)O[C@H]1CO)[C@@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 GUBGYTABKSRVRQ-YOLKTULGSA-N 0.000 claims description 51
- WQZGKKKJIJFFOK-GASJEMHNSA-N D-Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims description 17
- 239000008103 glucose Substances 0.000 claims description 17
- 238000002156 mixing Methods 0.000 claims description 14
- 239000000047 product Substances 0.000 claims description 13
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 10
- KDLHZDBZIXYQEI-UHFFFAOYSA-N palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 10
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 10
- 239000005092 Ruthenium Substances 0.000 claims description 7
- KJTLSVCANCCWHF-UHFFFAOYSA-N ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims description 7
- 229910052707 ruthenium Inorganic materials 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 6
- 238000004587 chromatography analysis Methods 0.000 claims description 5
- 150000002431 hydrogen Chemical class 0.000 claims description 5
- 229910044991 metal oxide Inorganic materials 0.000 claims description 5
- 150000004706 metal oxides Chemical class 0.000 claims description 5
- 229910052759 nickel Inorganic materials 0.000 claims description 5
- 229910052763 palladium Inorganic materials 0.000 claims description 5
- 229910052697 platinum Inorganic materials 0.000 claims description 5
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 5
- 229910052703 rhodium Inorganic materials 0.000 claims description 5
- 239000010948 rhodium Substances 0.000 claims description 5
- -1 saccharide alcohols Chemical class 0.000 claims description 4
- 239000007795 chemical reaction product Substances 0.000 claims description 2
- 230000001276 controlling effect Effects 0.000 claims description 2
- 125000002791 glucosyl group Chemical group C1([C@H](O)[C@@H](O)[C@H](O)[C@H](O1)CO)* 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 description 15
- WQZGKKKJIJFFOK-VFUOTHLCSA-N β-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 description 15
- 239000012530 fluid Substances 0.000 description 10
- 229910052751 metal Inorganic materials 0.000 description 9
- 239000002184 metal Substances 0.000 description 9
- 238000000926 separation method Methods 0.000 description 9
- 108090000790 Enzymes Proteins 0.000 description 8
- 102000004190 Enzymes Human genes 0.000 description 8
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- MEIRRNXMZYDVDW-MQQKCMAXSA-N (2E,4E)-hexa-2,4-dien-1-ol Chemical compound C\C=C\C=C\CO MEIRRNXMZYDVDW-MQQKCMAXSA-N 0.000 description 3
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- 239000000956 alloy Substances 0.000 description 2
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- REDXJYDRNCIFBQ-UHFFFAOYSA-N aluminium(3+) Chemical class [Al+3] REDXJYDRNCIFBQ-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
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- YXFVVABEGXRONW-UHFFFAOYSA-N toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 2
- 229910052723 transition metal Inorganic materials 0.000 description 2
- 150000003624 transition metals Chemical class 0.000 description 2
- UPYPTOCXMIWHSG-UHFFFAOYSA-N 1-dodecylsulfanyldodecane Chemical compound CCCCCCCCCCCCSCCCCCCCCCCCC UPYPTOCXMIWHSG-UHFFFAOYSA-N 0.000 description 1
- 241000276438 Gadus morhua Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
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- 125000003071 maltose group Chemical group 0.000 description 1
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- OZAIFHULBGXAKX-UHFFFAOYSA-N precursor Substances N#CC(C)(C)N=NC(C)(C)C#N OZAIFHULBGXAKX-UHFFFAOYSA-N 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000001953 recrystallisation Methods 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Abstract
The present invention provides a method and a system for purifying trehalose from a mixture containing trehalose and impurity saccharide, wherein the mixture contacts hydrogen in a micro reactor to generate a hydrogenation reaction so as to reduce the impurity saccharide into sugar alcohol to obtain a hydrogenation product containing trehalose and sugar alcohol, and the trehalose is separated from the hydrogenation product. With the method, trehalose can be effectively purified from the mixture containing trehalose and impurity saccharide.
Description
Technical field
The present invention relates to the sugar industry technical field, particularly the method and system of Purifing Trehalose from comprise trehalose and assorted sugared mixture.
Background technology
Trehalose (Trehalose) is with α by two glucose molecules; α-1; a kind of non-reducing disaccharide that the 1-glycosidic link forms; colourless odorless; there is very strong thermostability, acid acceptance and chemical stability, the biological components such as protein, nucleic acid, cytolemma are had to very strong stabilization, have the good reputation of " sugar of life "; when live body is subject to ambient pressure (dry, freeze, osmotic pressure etc.), provide protection is arranged, be unique by the U.S. FDA authentication, be safe functional oligose.
The research of both at home and abroad trehalose being produced is synthetic to enzyme process from microorganism extraction process, fermentation method, all, constantly improving production technique, enhances productivity.And the enzyme process trehalose synthesis becomes the main stream approach that trehalose is produced gradually, it is that to take glucose, maltose or starch etc. be substrate that enzyme transforming process is produced trehalose, by the enzyme system effect synthetic relevant with trehalose, changes into trehalose.According to the difference of enzyme system, enzyme transforming process is divided into again three kinds of Starch phosphorylase system two-step catalysis approach, non-phosphorylating enzyme system two-step catalysis approach, TreP one step catalysis approach.Wherein, TreP one step catalysis approach be by the TreP of treS genes encoding by transglycosylation in molecule α, the maltose that α-Isosorbide-5-Nitrae glycosidic link connects is converted into α, the trehalose that α-1,1 glycosidic link connects.General TreP one step catalysis approach also is attended by by product glucose and the complete maltose of unreacted exists, and in conjunction with corresponding separation means, obtains the trehalose product.
What in industrial production, the separating technology of trehalose mostly adopted at present is chromatographic separation technology, its key step comprises: the trehalose mixed solution is through the gac continuous stripping with after H-and the desalination of OH+ type ion exchange resin, utilize two or more chromatographic processes by combination again, as ion exchange column chromatography with by the column chromatography fractional separation that the column chromatography of gac or silica gel combines, finally utilize crystallization or recrystallization by the trehalose fractional crystallization out.
Yet, at present the separation and purification of trehalose still remained to be improved.
Summary of the invention
The present invention one of is intended to solve the problems of the technologies described above at least to a certain extent or at least provides a kind of useful business to select.For this reason, one object of the present invention be to propose a kind of from comprise trehalose and assorted sugared mixture the means of Purifing Trehalose.
In a first aspect of the present invention, the present invention proposes a kind of from comprise trehalose and assorted sugared mixture the method for Purifing Trehalose.According to embodiments of the invention, the method comprises: in microreactor, described mixture is contacted with hydrogen, in order to hydrogenation reaction occurs, make described assorted sugar be reduced to sugar alcohol, thereby obtain the hydrogenation products that contains the marine alga Saccharide and saccharide alcohols; And separate trehalose from described hydrogenation products.The present invention is based on the contriver and first micro-fluidic hydrogen addition technology is incorporated in the carbohydrate hydrogenation and completes.The contriver is through a large amount of research, be surprised to find that by utilizing microreactor, can complete the hydrogenation reaction that comprises the assorted sugar in trehalose and assorted sugared mixture, thus, the separation problem of trehalose and assorted sugar (for example maltose, glucose) can be changed into to separating of trehalose and sugar alcohol (for example maltose alcohol, sorbyl alcohol), improved the polarity difference between material, reduce separating difficulty, the sugar of simultaneously mixing changes sugar alcohol into, improve the utility value of assorted sugar, solved wasting of resources problem.In addition, utilize microreactor to complete hydrogenation reaction, the advantages such as mass-and heat-transfer speed is fast, specific surface area is high, reaction conditions is gentleer, easy control, the efficiency of raising hydrogenation reaction, strengthen the security of hydrogenation reaction.
According to embodiments of the invention, the method can also have following additional technical feature:
According to one embodiment of present invention, described assorted sugar comprises at least one that is selected from glucose and maltose.
According to one embodiment of present invention, described trehalose and the assorted sugared mixture of comprising is for by contacting maltose the reaction product obtained with TreP.
According to one embodiment of present invention, described hydrogenation reaction is to carry out at the temperature of 25 ~ 100 degrees centigrade.Preferably, described hydrogenation reaction is to carry out at the temperature of 50 ~ 80 degrees centigrade.According to one embodiment of present invention, the pressure of described hydrogen is 1 ~ 4MPa.Preferably, method according to claim 6, is characterized in that, the pressure of described hydrogen is 1 ~ 2MPa.According to one embodiment of present invention, the described trehalose that comprises is 10 ~ 50 (w/v) % with the solute concentration of the sugared mixture of mixing, and the described trehalose that comprises passes through described microreactor according to one embodiment of present invention with the flow velocity of sugared mixture with 0.2 ~ 1 ml/min of mixing, be provided with catalyzer in described microreactor, described catalyzer comprises at least one that is selected from nickel, rhodium, palladium, platinum, ruthenium and derivative thereof, and described derivative is for being selected from metal oxide.
Thus, according to a particular embodiment of the invention, in trehalose separation method of the present invention, microreactor can be comprised of one or more microchannels, and the width of described microchannel is the 1-1000 micron, preferred 100-500 micron, and the degree of depth is the 10-100 micron; The effect of described microchannel provides the working fluid flowing-path; Described microreactor also comprises micro mixer for gas-liquid two-phase is mixed; Described micro mixer comprises the mixing device of the shapes such as T shape or Y type.According to a particular embodiment of the invention, microreactor hydrogenation reaction temperature is 25-100 ℃, preferably 50-80 ℃; Described working fluid concentration 10-50 % (w/v), described working fluid flow velocity is 0.2-1 mL/min, preferably 0.4-0.6 mL/min; Described hydrogen pressure is 1-4 Mpa, preferably is less than 2 Mpa.In addition, according to a particular embodiment of the invention, catalyst for hydrogenation can be transition-metal catalyst, comprise the rare precious metals such as nickel, rhodium, palladium, platinum, ruthenium, and the rare metal derivative, as rare metal oxide, carried non-crystal alloy catalyst, loaded nano particle metal catalyst.According to a particular embodiment of the invention, in microreactor, catalyst loading can be 0.1-5 % (w/v), and can adopt content of metal is 0.1-50 wt%, preferably the loaded catalyst of 1-10 wt%.
In addition, according to embodiments of the invention, can separate trehalose from described hydrogenation products by chromatography.Can adopt any chromatographic process, for example comprise ion exchange column chromatography or in conjunction with simulation moving-bed more efficient chromatography separating method.
In a second aspect of the present invention, the present invention proposes a kind of for the system from comprising trehalose and the sugared mixture Purifing Trehalose of mixing.Concrete, with reference to figure 1 ~ 3, this system comprises: microreactor 100 and tripping device 200.According to embodiments of the invention, limit the hydrogenation space in described microreactor, for making described mixture, with hydrogen, contact, in order to hydrogenation reaction occurs, make described assorted sugar be reduced to sugar alcohol, thereby obtain the hydrogenation products that contains the marine alga Saccharide and saccharide alcohols.According to embodiments of the invention, described tripping device is connected with described microreactor, for from described hydrogenation products, separating trehalose.Thus, utilize according to an embodiment of the invention for can effectively implementing foregoing for the method from comprising trehalose and the sugared mixture Purifing Trehalose of mixing from comprising trehalose and the system of the sugared mixture Purifing Trehalose of mixing.Thus, by utilizing microreactor, can complete the hydrogenation reaction that comprises the assorted sugar in trehalose and assorted sugared mixture, thus, the separation problem of trehalose and assorted sugar (for example maltose, glucose) can be changed into to separating of trehalose and sugar alcohol (for example maltose alcohol, sorbyl alcohol), improve the polarity difference between material, reduce separating difficulty, the sugar of simultaneously mixing changes sugar alcohol into, has improved the utility value of assorted sugar, has solved wasting of resources problem.In addition, utilize microreactor to complete hydrogenation reaction, the advantages such as mass-and heat-transfer speed is fast, specific surface area is high, reaction conditions is gentleer, easy control, the efficiency of raising hydrogenation reaction, strengthen the security of hydrogenation reaction.
According to embodiments of the invention, this system can also have following additional technical feature:
In one embodiment of the invention, further comprise: premixed device 300, described premixed device is connected with described microreactor, for to described hydrogen with comprise trehalose and after assorted sugared mixture is pre-mixed, resulting mixture is supplied to described microreactor, wherein, described premixed device comprises: hydrogen inlet, and described hydrogen inlet is for supplying with hydrogen to described premixed device; The working liquid entrance, described working liquid entrance is for supplying with described trehalose and the assorted sugared mixture of comprising to described premixed device.
In one embodiment of the invention, further comprise: trehalose synthesizer 400 is provided with TreP in described trehalose synthesizer, for by maltose is contacted with TreP, obtaining described trehalose and the assorted sugared mixture of comprising.
In one embodiment of the invention, further comprise temperature-control device 500, described temperature-control device is for controlling the temperature of described microreactor.Preferably, described temperature-control device is oil bath device.
In one embodiment of the invention, described microreactor comprises at least one microchannel, and the width of described microchannel is the 1-1000 micron, and the degree of depth is 10 ~ 100 microns.Preferably, the width of described microreactor is 100 ~ 500 microns.Thus, according to a particular embodiment of the invention, in trehalose separation method of the present invention, microreactor can be comprised of one or more microchannels, and the width of described microchannel is the 1-1000 micron, preferred 100-500 micron, and the degree of depth is the 10-100 micron; The effect of described microchannel provides the working fluid flowing-path; Described microreactor also comprises micro mixer for gas-liquid two-phase is mixed; Described micro mixer comprises the mixing device of the shapes such as T shape or Y type.According to a particular embodiment of the invention, microreactor hydrogenation reaction temperature is 25-100 ℃, preferably 50-80 ℃; Described working fluid concentration 10-50 % (w/v), described working fluid flow velocity is 0.2-1 mL/min, preferably 0.4-0.6 mL/min; Described hydrogen pressure is 1-4 Mpa, preferably is less than 2 Mpa.In addition, according to a particular embodiment of the invention, catalyst for hydrogenation can be transition-metal catalyst, comprise the rare precious metals such as nickel, rhodium, palladium, platinum, ruthenium, and the rare metal derivative, as rare metal oxide, carried non-crystal alloy catalyst, loaded nano particle metal catalyst.According to a particular embodiment of the invention, in microreactor, catalyst loading can be 0.1-5 % (w/v), and can adopt content of metal is 0.1-50 wt%, preferably the loaded catalyst of 1-10 wt%.
In one embodiment of the invention, described tripping device is suitable for separating trehalose by chromatography from described hydrogenation products.
Additional aspect of the present invention and advantage part in the following description provide, and part will become obviously from the following description, or recognize by practice of the present invention.
In addition, it should be noted that, unless otherwise clearly defined and limited, broad understanding should be done in the term term such as " be connected ", for example, can be to be fixedly connected with, and can be also to removably connect, or connect integratedly; Can be mechanical connection, can be also to be electrically connected to; Can be directly to be connected, also can indirectly be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, can understand as the case may be above-mentioned term concrete meaning in the present invention.
The accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage are from obviously and easily understanding becoming the description of embodiment in conjunction with following accompanying drawing, wherein:
Fig. 1 is according to an embodiment of the invention for the structural representation from comprising trehalose and the sugared mixture Purifing Trehalose system of mixing;
Fig. 2 be according to the present invention another embodiment for the structural representation from comprising trehalose and assorted sugared mixture Purifing Trehalose system; And
Fig. 3 is in accordance with another embodiment of the present invention for the structural representation from comprising trehalose and the sugared mixture Purifing Trehalose system of mixing.
Embodiment
Below describe embodiments of the invention in detail, these embodiment are intended to for explaining the present invention, and can not be interpreted as limitation of the present invention.
Embodiment 1
(1) preparation of trehalose and other assorted sugared mixed solutions
The 20 % maltose of take are substrate, utilize TreP, at 25 ℃, under pH 7.0 conditions, catalysis maltose, obtain the mixed solution that comprises trehalose and glucose, 10 % that TreP enzyme dosage is maltose substrate quality, after enzymic catalytic reaction 20 h, in reaction solution, composition is 70 % trehaloses, the maltose that 22 % unreacteds are complete and the glucose by product of 8 %.
(2) loaded nano particle metal catalyst preparation
The title complex that loaded nano particle metal catalyst comprises dodecyl thioether and ruthenium (n-dodecylsul de-Ru), n-dodecylsul de-Ru (NDS-Ru) catalyzer adopts thermal decomposition method to be worth.At first, all glassware all needs to use chloroazotic acid to soak to remove reducing substances residual in Glass Containers.Ligand compound [CH in there-necked flask
3(CH
2)
11]
2s and ruthenium metal precursor Ru (cod) (cot) are dissolved in toluene with the 5:1 molar ratio, 60 ℃ of reaction 1 h of water-bath.Gained NDS-Ru catalyzer, its particle diameter is 4 ± 0.5 nm.
(3) sorbyl alcohol and maltose alcohol detection method
The HPLC method: liquid phase equipment (DIONEX-U3000), be equipped with (RI-101) differential detector and HP-Amino chromatographic column, mobile phase ratio is acetonitrile: water=65:35, column temperature: 30 ℃, flow velocity: 1.0 mL/min, working time 25min.
(4) glucose hydrogenation
In the hydrogenation microreactor, first pass into the air in 4-5 metathesis reactor of hydrogen, flow velocity with 0.4 mL/ min passes into 50 %(w/v again) glucose solution of concentration, the NDS-Ru catalyst loading is in whole length of described microreactor, keeping hydrogen pressure is 2 Mpa, keeps 60 ℃ of constant temperature oil baths.Hydrogen and glucose solution pass through micro mixer, microreactor successively, and in the parameter generation hydrogenation reaction according to listed in table 1, finally by discharge hole for discharge for separating of detection, result is as shown in table 1.
Embodiment 2 hydrogenation of maltose
According to the method for embodiment 1, just adopting 30 % maltose is working fluid, make maltose in microreactor according to parameter generation hydrogenation reaction listed in table 1, result is as shown in table 1.
Embodiment 3
According to the method for embodiment 1, just adopting the mixture of the maltose that comprises 27 wt% glucose and 73 wt% is working fluid, make glucose and maltose mixture in microreactor according to parameter generation hydrogenation reaction listed in table 1, result is as shown in table 1.
Table 1
| Embodiment | Working fluid | Temperature/℃ | Hydrogen pressure/Mpa | Working fluid flow velocity mL/min | Transformation efficiency/% |
| 1 | Glucose | 60 | 2 | 0.4 | 99.9 |
| 2 | Maltose | 60 | 2 | 0.4 | 99.9 |
| 3 | Glucose and maltose mixture | 60 | 2 | 0.4 | 99.9 |
As can be seen from Table 1, utilize microreactor effectively glucose, maltose and the mixing of the two to be converted into to corresponding sugar alcohol, thereby be convenient to the later separation Purifing Trehalose.
In the description of this specification sheets, the description of reference term " embodiment ", " some embodiment ", " example ", " concrete example " or " some examples " etc. means to be contained at least one embodiment of the present invention or example in conjunction with specific features, structure, material or the characteristics of this embodiment or example description.In this manual, the schematic statement of above-mentioned term not necessarily referred to identical embodiment or example.And the specific features of description, structure, material or characteristics can be with suitable mode combinations in any one or more embodiment or example.
Although the above has illustrated and has described embodiments of the invention, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, those of ordinary skill in the art is not in the situation that break away from principle of the present invention and aim can be changed above-described embodiment within the scope of the invention, modification, replacement and modification.
Claims (19)
1. the method for a Purifing Trehalose from comprise trehalose and assorted sugared mixture, is characterized in that, comprising:
In microreactor, described mixture is contacted with hydrogen, in order to hydrogenation reaction occurs, make described assorted sugar be reduced to sugar alcohol, thereby obtain the hydrogenation products that contains the marine alga Saccharide and saccharide alcohols; And
Separate trehalose from described hydrogenation products.
2. method according to claim 1, is characterized in that, described assorted sugar comprises at least one that is selected from glucose and maltose.
3. method according to claim 2, is characterized in that, described trehalose and the assorted sugared mixture of comprising is for by contacting maltose the reaction product obtained with TreP.
4. method according to claim 1, is characterized in that, described hydrogenation reaction is to carry out at the temperature of 25 ~ 100 degrees centigrade.
5. method according to claim 1, is characterized in that, described hydrogenation reaction is to carry out at the temperature of 50 ~ 80 degrees centigrade.
6. method according to claim 1, is characterized in that, the pressure of described hydrogen is 1 ~ 4MPa.
7. method according to claim 6, is characterized in that, the pressure of described hydrogen is 1 ~ 2MPa.
8. method according to claim 1, it is characterized in that, the described trehalose that comprises is 10 ~ 50 (w/v) % with the solute concentration of the sugared mixture of mixing, and the described trehalose that comprises passes through described microreactor with the flow velocity of sugared mixture with 0.2 ~ 1 ml/min of mixing.
9. method according to claim 1, is characterized in that, in described microreactor, is provided with catalyzer, and described catalyzer comprises at least one that is selected from nickel, rhodium, palladium, platinum, ruthenium and derivative thereof, and described derivative is for being selected from metal oxide.
10. method according to claim 1, is characterized in that, by chromatography, from described hydrogenation products, separates trehalose.
11. one kind for the system from comprising trehalose and assorted sugared mixture Purifing Trehalose, it is characterized in that, comprising:
Microreactor, limit the hydrogenation space in described microreactor, for making described mixture, with hydrogen, contact, in order to hydrogenation reaction occurs, makes described assorted sugar be reduced to sugar alcohol, thereby obtain the hydrogenation products that contains the marine alga Saccharide and saccharide alcohols; And
Tripping device, described tripping device is connected with described microreactor, for from described hydrogenation products, separating trehalose.
12. system according to claim 11, is characterized in that, further comprises:
Premixed device, described premixed device is connected with described microreactor, for to described hydrogen with comprise trehalose and after assorted sugared mixture is pre-mixed, resulting mixture is supplied to described microreactor,
Wherein,
Described premixed device comprises:
Hydrogen inlet, described hydrogen inlet is for supplying with hydrogen to described premixed device;
The working liquid entrance, described working liquid entrance is for supplying with described trehalose and the assorted sugared mixture of comprising to described premixed device.
13. system according to claim 12, is characterized in that, further comprises:
The trehalose synthesizer, be provided with TreP in described trehalose synthesizer, for by maltose is contacted with TreP, obtaining described trehalose and the assorted sugared mixture of comprising.
14. system according to claim 11, is characterized in that, further comprises temperature-control device, described temperature-control device is for controlling the temperature of described microreactor.
15. system according to claim 14, is characterized in that, described temperature-control device is oil bath device.
16. system according to claim 11, is characterized in that, described microreactor comprises at least one microchannel, and the width of described microchannel is the 1-1000 micron, and the degree of depth is 10 ~ 100 microns.
17. system according to claim 16, is characterized in that, the width of described microreactor is 100 ~ 500 microns.
18. system according to claim 1, is characterized in that, in described microreactor, is provided with catalyzer, described catalyzer comprises at least one that is selected from nickel, rhodium, palladium, platinum, ruthenium and derivative thereof, and described derivative is for being selected from metal oxide.
19. system according to claim 1, is characterized in that, described tripping device is suitable for separating trehalose by chromatography from described hydrogenation products.
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| CN104478949A (en) * | 2014-11-24 | 2015-04-01 | 华东理工大学 | Chromatographic separation method of trehalose and maltose |
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