CN219972321U - D-psicose apparatus for producing - Google Patents
D-psicose apparatus for producing Download PDFInfo
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- CN219972321U CN219972321U CN202321591561.4U CN202321591561U CN219972321U CN 219972321 U CN219972321 U CN 219972321U CN 202321591561 U CN202321591561 U CN 202321591561U CN 219972321 U CN219972321 U CN 219972321U
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- membrane filter
- outlet
- resin column
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- BJHIKXHVCXFQLS-PUFIMZNGSA-N D-psicose Chemical compound OC[C@@H](O)[C@@H](O)[C@@H](O)C(=O)CO BJHIKXHVCXFQLS-PUFIMZNGSA-N 0.000 title claims abstract description 29
- 239000012528 membrane Substances 0.000 claims abstract description 60
- 239000000919 ceramic Substances 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 40
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000002425 crystallisation Methods 0.000 claims abstract description 30
- 230000008025 crystallization Effects 0.000 claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims abstract description 27
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 26
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 claims abstract description 23
- RFSUNEUAIZKAJO-ARQDHWQXSA-N Fructose Chemical compound OC[C@H]1O[C@](O)(CO)[C@@H](O)[C@@H]1O RFSUNEUAIZKAJO-ARQDHWQXSA-N 0.000 claims abstract description 17
- 108090000790 Enzymes Proteins 0.000 claims abstract description 16
- 102000004190 Enzymes Human genes 0.000 claims abstract description 16
- 229930091371 Fructose Natural products 0.000 claims abstract description 16
- 239000005715 Fructose Substances 0.000 claims abstract description 16
- 239000013078 crystal Substances 0.000 claims abstract description 12
- 238000003860 storage Methods 0.000 claims abstract description 12
- 238000000108 ultra-filtration Methods 0.000 claims description 20
- 239000011347 resin Substances 0.000 claims description 18
- 229920005989 resin Polymers 0.000 claims description 18
- 238000001179 sorption measurement Methods 0.000 claims description 16
- 238000000967 suction filtration Methods 0.000 claims description 15
- 239000003957 anion exchange resin Substances 0.000 claims description 8
- 239000003729 cation exchange resin Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 6
- 239000012535 impurity Substances 0.000 abstract description 10
- 238000000034 method Methods 0.000 abstract description 9
- 239000000243 solution Substances 0.000 description 42
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 238000009776 industrial production Methods 0.000 description 6
- 239000002699 waste material Substances 0.000 description 5
- 238000004042 decolorization Methods 0.000 description 4
- 238000010612 desalination reaction Methods 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 229930006000 Sucrose Natural products 0.000 description 2
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 238000011031 large-scale manufacturing process Methods 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000002791 soaking Methods 0.000 description 2
- 239000005720 sucrose Substances 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- RFSUNEUAIZKAJO-VRPWFDPXSA-N D-Fructose Natural products OC[C@H]1OC(O)(CO)[C@@H](O)[C@@H]1O RFSUNEUAIZKAJO-VRPWFDPXSA-N 0.000 description 1
- WQZGKKKJIJFFOK-IVMDWMLBSA-N D-allopyranose Chemical compound OC[C@H]1OC(O)[C@H](O)[C@H](O)[C@@H]1O WQZGKKKJIJFFOK-IVMDWMLBSA-N 0.000 description 1
- LKDRXBCSQODPBY-JDJSBBGDSA-N D-allulose Chemical compound OCC1(O)OC[C@@H](O)[C@@H](O)[C@H]1O LKDRXBCSQODPBY-JDJSBBGDSA-N 0.000 description 1
- 108030002106 D-psicose 3-epimerases Proteins 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012527 feed solution Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Saccharide Compounds (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The utility model relates to a D-psicose production device, which comprises a reaction kettle, wherein a fructose solution tank and an enzyme solution storage tank are respectively communicated with an upper feed inlet of the reaction kettle through a pipeline, a ceramic membrane filter is communicated with a lower discharge outlet of the reaction kettle through a pipeline, an ion exchange resin column is communicated with a clear liquid outlet of the ceramic membrane filter through a pipeline, a simulated moving bed is communicated with an outlet of the ion exchange resin column through a pipeline, a feed liquid outlet of the simulated moving bed is communicated with a crystallization kettle through a pipeline, a seed crystal tank is communicated with an inlet of the crystallization kettle through a pipeline, and a finished product tank is communicated with a bottom outlet of the crystallization kettle through a pipeline. The conversion liquid obtained after the fructose solution reacts with the enzyme solution can remove insoluble impurities in the feed liquid through the ceramic membrane filter, so that the purity of the product is improved, the quality of the product is higher, and meanwhile, the residence time of the conversion liquid in the ceramic membrane filter is short, and the process period is shortened.
Description
Technical Field
The utility model relates to the technical field of psicose production, in particular to a D-psicose production device.
Background
D-psicose is a functional rare sugar. D-psicose, english name D-allose, molecular formula C 6 H 12 O 6 The relative molecular mass is 180.16g/mol, and the epimer of D-fructose at the C-3 position is adopted. It is a white, odorless crystalline powder. D-psicose has 70% sweetness of sucrose, but has low calorie, and is a good substitute of sucrose.
Chinese patent CN217757509U discloses a device for improving the production efficiency of D-psicose, which adjusts the addition amount of enzyme liquid according to the conversion rate of D-psicose, so that the conversion rate of D-psicose reaches an optimal value, and the waste of fructose substrate is avoided, but activated carbon is used for decoloring, the consumption of activated carbon is large, and the material retention time is long, so that the whole production period is prolonged, the impurity removing effect is poor, and the quality of the product is affected.
Disclosure of Invention
The technical problems to be solved by the utility model are as follows: aiming at the defects existing in the prior art, the device for producing the D-psicose is provided, the production period is short, and the product quality is high.
In order to solve the technical problems, the technical scheme of the utility model is as follows:
the utility model provides a D-psicose apparatus for producing, includes reation kettle, reation kettle's upper portion feed inlet has fructose solution jar and enzyme liquid storage tank through the pipeline intercommunication respectively, reation kettle's lower part discharge gate has ceramic membrane filter through the pipeline intercommunication, ceramic membrane filter's clear liquid export has the ion exchange resin post through the pipeline intercommunication, the export of ion exchange resin post has the simulated moving bed through the pipeline intercommunication, the feed liquid export of simulated moving bed is through pipeline intercommunication to crystallization kettle, crystallization kettle's entry has the seed crystal jar through the pipeline intercommunication, crystallization kettle's bottom export has the finished product jar through the pipeline intercommunication.
As an improved technical scheme, an ultrafiltration membrane filter is arranged between the ceramic membrane filter and the ion exchange resin column, and an inlet and an outlet of the ultrafiltration membrane filter are respectively communicated with the ion exchange resin column and the ceramic membrane filter.
As an improved technical scheme, the separation aperture of the ultrafiltration membrane filter is between 10 and 20 nm.
As an improved technical scheme, the concentrated solution outlet of the ceramic membrane filter is communicated with the inlet of the enzyme solution storage tank through a pipeline.
As an improved technical scheme, a macroporous adsorption resin column is arranged between the simulated moving bed and the crystallization kettle, and the inlet and outlet of the macroporous adsorption resin column are respectively communicated with the crystallization kettle and the simulated moving bed.
As an improved technical scheme, the separation pore diameter of the ceramic membrane filter is 20-100 nm.
As the preferable technical scheme, the outlet of the crystallization kettle is communicated with a suction filtration tank through a pipeline, the upper outlet of the suction filtration tank is communicated with a vacuum pump through a pipeline, and the lower outlet of the suction filtration tank is communicated to the finished product tank through a pipeline.
The ion exchange resin column comprises a cation exchange resin column and an anion exchange resin column which are sequentially communicated.
And a recovery liquid outlet of the simulated moving bed is communicated to the fructose solution tank through a pipeline.
Due to the adoption of the technical scheme, the utility model has the beneficial effects that:
the utility model relates to a D-psicose production device, which comprises a reaction kettle, wherein a fructose solution tank and an enzyme solution storage tank are respectively communicated with an upper feed inlet of the reaction kettle through a pipeline, a ceramic membrane filter is communicated with a lower discharge outlet of the reaction kettle through a pipeline, an ion exchange resin column is communicated with a clear liquid outlet of the ceramic membrane filter through a pipeline, a simulated moving bed is communicated with an outlet of the ion exchange resin column through a pipeline, a feed liquid outlet of the simulated moving bed is communicated with a crystallization kettle through a pipeline, a seed crystal tank is communicated with an inlet of the crystallization kettle through a pipeline, and a finished product tank is communicated with a bottom outlet of the crystallization kettle through a pipeline. The conversion liquid obtained after the fructose solution reacts with the enzyme solution can remove insoluble impurities in the feed liquid through the ceramic membrane filter, so that the purity of the product is improved, the quality of the product is higher, and meanwhile, the residence time of the conversion liquid in the ceramic membrane filter is short, and the process period is shortened. The ion exchange resin column comprises a cation exchange resin column and an anion exchange resin column which are sequentially communicated, the decontaminated feed liquid enters the cation exchange resin column and the anion exchange resin column for desalination, the conductivity of the feed liquid can be reduced from 2000us/cm to less than 50us/cm, the desalination effect is obvious, the resin in the ion exchange resin column can be repeatedly used for multiple times, the operation is easy, the safety is high, the industrial production is easy to realize, the obtained desalinated liquid can be directly separated by a simulated moving bed without concentration, the production cost is reduced, and the process period is shortened.
An ultrafiltration membrane filter is arranged between the ceramic membrane filter and the ion exchange resin column, and an inlet and an outlet of the ultrafiltration membrane filter are respectively communicated with the ion exchange resin column and the ceramic membrane filter. The ultrafiltration membrane filter is adopted, so that macromolecular organic matters and partial macromolecular impurities in the feed liquid can be removed, the feed liquid is further purified, the purity of the product is improved, meanwhile, the ultrafiltration membrane filter has small occupied area, easy operation and high safety, large-scale production is pollution-free, the investment of environmental protection cost can be reduced, and industrial production is easy to realize.
The separation aperture of the ultrafiltration membrane filter is between 10 and 20nm, and the impurity removal effect is good.
And the concentrated solution outlet of the ceramic membrane filter is communicated with the inlet of the enzyme solution storage tank through a pipeline. The ceramic membrane concentrated solution can be recycled, and the ceramic membrane concentrated solution is added into the enzyme solution storage tank to enter the reaction system again for synthesizing the D-psicose, so that the fermentation cost can be reduced to a certain extent, the ceramic membrane filtration can realize continuous production, and the equipment has small occupied area, easy operation and high safety, and is easy to realize industrial production.
And a macroporous adsorption resin column is arranged between the simulated moving bed and the crystallization kettle, and the inlet and outlet of the macroporous adsorption resin column are respectively communicated with the crystallization kettle and the simulated moving bed. The macroporous adsorption resin column is adopted for decolorization, the clarity of the decolorized feed liquid is good, compared with activated carbon decolorization, the macroporous adsorption resin column can be regenerated and recycled only by short-time soaking, the operation is simple, meanwhile, the occupied area of the macroporous adsorption resin column is small, the operation is easy, no pollution is caused, the production cost is reduced, and meanwhile, the production of dangerous waste is reduced, so that the method has certain advantages in the aspects of environmental protection and occupational health.
The separation aperture of the ceramic membrane filter is 20-100 nm, the impurity removal effect is good, and the purity of the product is improved.
The outlet of the crystallization kettle is communicated with a suction filtration tank through a pipeline, the upper outlet of the suction filtration tank is communicated with a vacuum pump through a pipeline, and the lower outlet of the suction filtration tank is communicated to the finished product tank through a pipeline. The D-psicose crystals can be rapidly separated and collected through suction filtration, the whole process period is shortened, and the finally obtained crystals have good crystal forms.
And a recovery liquid outlet of the simulated moving bed is communicated to the fructose solution tank through a pipeline, and the recovery liquid is recycled, so that the waste of raw materials is avoided.
Drawings
The utility model will be further described with reference to the drawings and examples.
FIG. 1 is a schematic diagram of an embodiment of the present utility model;
wherein: 1. a reaction kettle; 2. a fructose solution tank; 3. an enzyme liquid storage tank; 4. a ceramic membrane filter; 5. an ion exchange resin column; 51. a cation exchange resin column; 52. an anion exchange resin column 51; 6. a simulated moving bed; 7. a crystallization kettle; 8. a seed tank; 9. a finished product tank; 10. an ultrafiltration membrane filter; 11. a macroporous adsorption resin column; 12. a suction filtration tank; 13. and a vacuum pump.
Detailed Description
The utility model is further illustrated in the following, in conjunction with the accompanying drawings and examples.
As shown in figure 1, a D-psicose production device comprises a reaction kettle 1, wherein a fructose solution tank 2 and an enzyme solution storage tank 3 are respectively communicated with an upper feed inlet of the reaction kettle 1 through a pipeline, a ceramic membrane filter 4 is communicated with a lower discharge outlet of the reaction kettle 1 through a pipeline, an ion exchange resin column 5 is communicated with a clear liquid outlet of the ceramic membrane filter 4 through a pipeline, a simulated moving bed 6 is communicated with an outlet of the ion exchange resin column 5 through a pipeline, a feed liquid outlet of the simulated moving bed 6 is communicated with a crystallization kettle 7 through a pipeline, a seed crystal tank 8 is communicated with an inlet of the crystallization kettle 7 through a pipeline, and a finished product tank 9 is communicated with a bottom outlet of the crystallization kettle 7 through a pipeline. The conversion liquid obtained after the fructose solution reacts with the enzyme solution can remove insoluble impurities in the feed liquid through the ceramic membrane filter 4, so that the purity of the product is improved, the quality of the product is higher, and meanwhile, the residence time of the conversion liquid in the ceramic membrane filter 4 is short, and the process period is shortened. The purified feed liquid enters the cation exchange resin column 51 and the anion exchange resin column 52 for desalination, the conductivity of the feed liquid can be reduced from 2000us/cm to less than 50us/cm, the desalination effect is obvious, the resin in the ion exchange resin column 5 can be repeatedly used, the operation is easy, the safety is high, the industrial production is easy to realize, and the obtained desalinated liquid can be directly separated by the simulated moving bed 6 without concentrating, so that the production cost is reduced, and the process period is shortened.
An ultrafiltration membrane filter 10 is arranged between the ceramic membrane filter 4 and the ion exchange resin column 5, and the inlet and outlet of the ultrafiltration membrane filter 10 are respectively communicated with the ion exchange resin column 5 and the ceramic membrane filter 4. The adoption of the ultrafiltration membrane filter 10 can remove macromolecular organic matters and partial macromolecular impurities in the feed liquid, so that the feed liquid is further purified, the purity of the product is improved, meanwhile, the ultrafiltration membrane filter 10 has small occupied area, easy operation and high safety, large-scale production has no pollution, the investment of environmental protection cost can be reduced, and the industrial production is easy to realize.
The separation aperture of the ultrafiltration membrane filter 10 is between 10 and 20nm, and the impurity removal effect is good.
The concentrated solution outlet of the ceramic membrane filter 4 is communicated with the inlet of the enzyme solution storage tank 3 through a pipeline. The ceramic membrane concentrated solution can be recycled, and the ceramic membrane concentrated solution is added into the enzyme solution storage tank 3 to enter the reaction system again for synthesizing the D-psicose, so that the fermentation cost can be reduced to a certain extent, the ceramic membrane filtration can realize continuous production, and the equipment has small occupied area, easy operation and high safety, and is easy to realize industrial production.
A macroporous adsorption resin column 11 is arranged between the simulated moving bed 6 and the crystallization kettle 7, and the inlet and outlet of the macroporous adsorption resin column 11 are respectively communicated with the crystallization kettle 7 and the simulated moving bed 6. The macroporous adsorption resin column 11 is adopted for decolorization, the clarity of the decolorized feed liquid is good, compared with activated carbon decolorization, the macroporous adsorption resin column 11 can be regenerated and recycled only by short-time soaking, the operation is simple, meanwhile, the occupied area of the macroporous adsorption resin column 11 is small, the operation is easy, no pollution is caused, the production cost is reduced, and meanwhile, the production of dangerous waste is reduced, so that the method has certain advantages in the aspects of environmental protection and occupational health.
The separation aperture of the ceramic membrane filter 4 is 20-100 nm, the impurity removal effect is good, and the purity of the product is improved.
The outlet of the crystallization kettle 7 is communicated with a suction filtration tank 12 through a pipeline, the upper outlet of the suction filtration tank 12 is communicated with a vacuum pump 13 through a pipeline, and the lower outlet of the suction filtration tank 12 is communicated to the finished product tank 9 through a pipeline. The D-psicose crystals can be rapidly separated and collected through suction filtration, the whole process period is shortened, and the finally obtained crystals have good crystal forms.
The recovery liquid outlet of the simulated moving bed 6 is communicated to the fructose solution tank 2 through a pipeline, and the recovery liquid is recycled, so that the waste of raw materials is avoided.
The working principle of the utility model is as follows:
the fructose solution and the D-psicose 3-epimerase enzyme solution are respectively added into a reaction kettle 1, a conversion solution is obtained after reaction, the conversion solution is respectively collected by a ceramic membrane filter 4, ceramic membrane clear solution and ceramic membrane concentrated solution are respectively transferred into a fructose solution tank 2 for reuse, the collected ceramic membrane clear solution is filtered by an ultrafiltration membrane filter 10, the ultrafiltration clear solution is collected, the ultrafiltration clear solution is filtered by an ion exchange resin column 5, the ion exchange resin column 5 in the embodiment is a cation exchange resin column 51 and an anion exchange resin column 52 which are connected in series, a desalted solution with the conductivity less than 50us/cm is obtained after passing through the cation exchange resin column 51 and the anion exchange resin column 52, the desalted solution is fed into a sequential simulated moving bed 6, the obtained D-psicose feed solution is fed into a macroporous adsorption resin column 11 to obtain a decolorized solution, the decolorized solution is fed into a crystallization kettle 7, the crystallization kettle 7 is communicated with a vacuum pump 13, when the collected ceramic membrane clear solution is concentrated to be more than 80% w/w solid content under the conditions of vacuum < -0.09MPa at 50-70 ℃, D-psicose seed crystal is added, and then the desalted solution is obtained after the desalting solution is pumped at a speed of 25 ℃ for 3 h.
It is to be understood that these examples are illustrative of the present utility model and are not intended to limit the scope of the present utility model. Furthermore, it should be understood that various changes and modifications can be made by one skilled in the art after reading the teachings of the present utility model, and such equivalents are intended to fall within the scope of the utility model as defined in the appended claims.
Claims (9)
1. A D-psicose production device, characterized in that: the device comprises a reaction kettle, wherein a fructose solution tank and an enzyme solution storage tank are respectively communicated with an upper feed inlet of the reaction kettle through a pipeline, a ceramic membrane filter is communicated with a lower discharge outlet of the reaction kettle through a pipeline, an ion exchange resin column is communicated with a clear liquid outlet of the ceramic membrane filter through a pipeline, a simulated moving bed is communicated with an outlet of the ion exchange resin column through a pipeline, a feed liquid outlet of the simulated moving bed is communicated with a crystallization kettle through a pipeline, a seed crystal tank is communicated with an inlet of the crystallization kettle through a pipeline, and a finished product tank is communicated with a bottom outlet of the crystallization kettle through a pipeline.
2. A D-psicose production device as claimed in claim 1, wherein: an ultrafiltration membrane filter is arranged between the ceramic membrane filter and the ion exchange resin column, and an inlet and an outlet of the ultrafiltration membrane filter are respectively communicated with the ion exchange resin column and the ceramic membrane filter.
3. A D-psicose production device as claimed in claim 2, characterized in that: the separation aperture of the ultrafiltration membrane filter is between 10 and 20 nm.
4. A D-psicose production device as claimed in claim 1, wherein: and the concentrated solution outlet of the ceramic membrane filter is communicated with the inlet of the enzyme solution storage tank through a pipeline.
5. A D-psicose production device as claimed in claim 1, wherein: and a macroporous adsorption resin column is arranged between the simulated moving bed and the crystallization kettle, and the inlet and outlet of the macroporous adsorption resin column are respectively communicated with the crystallization kettle and the simulated moving bed.
6. A D-psicose production device as claimed in claim 1, wherein: the separation aperture of the ceramic membrane filter is 20-100 nm.
7. A D-psicose production device as claimed in claim 1, wherein: the outlet of the crystallization kettle is communicated with a suction filtration tank through a pipeline, the upper outlet of the suction filtration tank is communicated with a vacuum pump through a pipeline, and the lower outlet of the suction filtration tank is communicated to the finished product tank through a pipeline.
8. A D-psicose production device as claimed in claim 1, wherein: the ion exchange resin column comprises a cation exchange resin column and an anion exchange resin column which are sequentially communicated.
9. A D-psicose production device as claimed in claim 1, wherein: and a recovery liquid outlet of the simulated moving bed is communicated to the fructose solution tank through a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321591561.4U CN219972321U (en) | 2023-06-20 | 2023-06-20 | D-psicose apparatus for producing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321591561.4U CN219972321U (en) | 2023-06-20 | 2023-06-20 | D-psicose apparatus for producing |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219972321U true CN219972321U (en) | 2023-11-07 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202321591561.4U Active CN219972321U (en) | 2023-06-20 | 2023-06-20 | D-psicose apparatus for producing |
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| Country | Link |
|---|---|
| CN (1) | CN219972321U (en) |
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2023
- 2023-06-20 CN CN202321591561.4U patent/CN219972321U/en active Active
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