CN220657493U - Device for preparing inositol triphosphate by using corn soaking water - Google Patents
Device for preparing inositol triphosphate by using corn soaking water Download PDFInfo
- Publication number
- CN220657493U CN220657493U CN202322302914.0U CN202322302914U CN220657493U CN 220657493 U CN220657493 U CN 220657493U CN 202322302914 U CN202322302914 U CN 202322302914U CN 220657493 U CN220657493 U CN 220657493U
- Authority
- CN
- China
- Prior art keywords
- communicated
- pipeline
- outlet
- tank
- inositol triphosphate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 59
- MMWCIQZXVOZEGG-HOZKJCLWSA-N [(1S,2R,3S,4S,5R,6S)-2,3,5-trihydroxy-4,6-diphosphonooxycyclohexyl] dihydrogen phosphate Chemical compound O[C@H]1[C@@H](O)[C@H](OP(O)(O)=O)[C@@H](OP(O)(O)=O)[C@H](O)[C@H]1OP(O)(O)=O MMWCIQZXVOZEGG-HOZKJCLWSA-N 0.000 title claims abstract description 46
- 240000008042 Zea mays Species 0.000 title claims abstract description 35
- 235000002017 Zea mays subsp mays Nutrition 0.000 title claims abstract description 35
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 title claims abstract description 29
- 235000005822 corn Nutrition 0.000 title claims abstract description 29
- 238000002791 soaking Methods 0.000 title abstract description 12
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims abstract description 46
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 30
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 28
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims abstract description 23
- 230000007062 hydrolysis Effects 0.000 claims abstract description 21
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 21
- 239000000047 product Substances 0.000 claims abstract description 21
- CDAISMWEOUEBRE-UHFFFAOYSA-N inositol Chemical compound OC1C(O)C(O)C(O)C(O)C1O CDAISMWEOUEBRE-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000000706 filtrate Substances 0.000 claims abstract description 14
- 239000001226 triphosphate Substances 0.000 claims abstract description 13
- 235000011178 triphosphate Nutrition 0.000 claims abstract description 13
- 239000003054 catalyst Substances 0.000 claims abstract description 9
- 239000012528 membrane Substances 0.000 claims description 36
- 238000001728 nano-filtration Methods 0.000 claims description 36
- 238000002425 crystallisation Methods 0.000 claims description 13
- 230000008025 crystallization Effects 0.000 claims description 13
- 238000002360 preparation method Methods 0.000 claims description 11
- 238000004821 distillation Methods 0.000 claims description 9
- 238000011010 flushing procedure Methods 0.000 claims description 9
- 239000008213 purified water Substances 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 claims description 6
- 235000009973 maize Nutrition 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 5
- 239000007791 liquid phase Substances 0.000 claims description 4
- 239000007790 solid phase Substances 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 13
- 230000008569 process Effects 0.000 abstract description 9
- 239000012535 impurity Substances 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 239000002994 raw material Substances 0.000 abstract description 5
- 230000009471 action Effects 0.000 abstract description 3
- 238000009776 industrial production Methods 0.000 abstract description 3
- 239000011949 solid catalyst Substances 0.000 abstract description 3
- 238000003860 storage Methods 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 239000011575 calcium Substances 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 5
- CDAISMWEOUEBRE-GPIVLXJGSA-N inositol Chemical compound O[C@H]1[C@H](O)[C@@H](O)[C@H](O)[C@H](O)[C@@H]1O CDAISMWEOUEBRE-GPIVLXJGSA-N 0.000 description 5
- 108010011619 6-Phytase Proteins 0.000 description 4
- SQUHHTBVTRBESD-UHFFFAOYSA-N Hexa-Ac-myo-Inositol Natural products CC(=O)OC1C(OC(C)=O)C(OC(C)=O)C(OC(C)=O)C(OC(C)=O)C1OC(C)=O SQUHHTBVTRBESD-UHFFFAOYSA-N 0.000 description 4
- IMQLKJBTEOYOSI-GPIVLXJGSA-N Inositol-hexakisphosphate Chemical compound OP(O)(=O)O[C@H]1[C@H](OP(O)(O)=O)[C@@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@@H]1OP(O)(O)=O IMQLKJBTEOYOSI-GPIVLXJGSA-N 0.000 description 4
- IMQLKJBTEOYOSI-UHFFFAOYSA-N Phytic acid Natural products OP(O)(=O)OC1C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C1OP(O)(O)=O IMQLKJBTEOYOSI-UHFFFAOYSA-N 0.000 description 4
- 229960000367 inositol Drugs 0.000 description 4
- 239000012452 mother liquor Substances 0.000 description 4
- 229940085127 phytase Drugs 0.000 description 4
- 229940068041 phytic acid Drugs 0.000 description 4
- 235000002949 phytic acid Nutrition 0.000 description 4
- 239000000467 phytic acid Substances 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- -1 Inositol phosphates Chemical class 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- 229920002472 Starch Polymers 0.000 description 2
- YDHWWBZFRZWVHO-UHFFFAOYSA-H [oxido-[oxido(phosphonatooxy)phosphoryl]oxyphosphoryl] phosphate Chemical compound [O-]P([O-])(=O)OP([O-])(=O)OP([O-])(=O)OP([O-])([O-])=O YDHWWBZFRZWVHO-UHFFFAOYSA-H 0.000 description 2
- 238000005903 acid hydrolysis reaction Methods 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 150000001982 diacylglycerols Chemical class 0.000 description 2
- 230000003834 intracellular effect Effects 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- 102000004169 proteins and genes Human genes 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000012958 reprocessing Methods 0.000 description 2
- 235000019698 starch Nutrition 0.000 description 2
- 239000008107 starch Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 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 description 1
- INAPMGSXUVUWAF-UOTPTPDRSA-N 1D-myo-inositol 1-phosphate Chemical compound O[C@H]1[C@H](O)[C@@H](O)[C@H](OP(O)(O)=O)[C@H](O)[C@@H]1O INAPMGSXUVUWAF-UOTPTPDRSA-N 0.000 description 1
- 102000014384 Type C Phospholipases Human genes 0.000 description 1
- 108010079194 Type C Phospholipases Proteins 0.000 description 1
- FENRSEGZMITUEF-ATTCVCFYSA-E [Na+].[Na+].[Na+].[Na+].[Na+].[Na+].[Na+].[Na+].[Na+].OP(=O)([O-])O[C@@H]1[C@@H](OP(=O)([O-])[O-])[C@H](OP(=O)(O)[O-])[C@H](OP(=O)([O-])[O-])[C@H](OP(=O)(O)[O-])[C@H]1OP(=O)([O-])[O-] Chemical compound [Na+].[Na+].[Na+].[Na+].[Na+].[Na+].[Na+].[Na+].[Na+].OP(=O)([O-])O[C@@H]1[C@@H](OP(=O)([O-])[O-])[C@H](OP(=O)(O)[O-])[C@H](OP(=O)([O-])[O-])[C@H](OP(=O)(O)[O-])[C@H]1OP(=O)([O-])[O-] FENRSEGZMITUEF-ATTCVCFYSA-E 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 210000004027 cell Anatomy 0.000 description 1
- 230000036755 cellular response Effects 0.000 description 1
- 235000013339 cereals Nutrition 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 210000000172 cytosol Anatomy 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002255 enzymatic effect Effects 0.000 description 1
- 230000007071 enzymatic hydrolysis Effects 0.000 description 1
- 238000006047 enzymatic hydrolysis reaction Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000000413 hydrolysate Substances 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 238000001727 in vivo Methods 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 235000021317 phosphate Nutrition 0.000 description 1
- 150000003905 phosphatidylinositols Chemical class 0.000 description 1
- 150000003906 phosphoinositides Chemical class 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229940083982 sodium phytate Drugs 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000003930 superacid Substances 0.000 description 1
- ZXAUZSQITFJWPS-UHFFFAOYSA-J zirconium(4+);disulfate Chemical compound [Zr+4].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O ZXAUZSQITFJWPS-UHFFFAOYSA-J 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses a device for preparing inositol triphosphate by using corn steep water, which relates to the technical field of corn steep water backwater utilization, wherein a resolving agent enters an anion exchange resin column to resolve the corn steep water backwater, the obtained resolving liquid enters a hydrolysis tank, inositol triphosphate is generated under the action of a catalyst, a solid catalyst and insoluble impurities are removed through a first filter, filtrate enters a first concentrator, concentrated solution enters a simulated moving bed to be separated, and an inositol triphosphate solution and a dilute phosphoric acid solution are obtained, wherein the inositol triphosphate solution is filtered again after being concentrated by a second concentrator, and the filtrate is crystallized, centrifuged and dried to obtain an inositol triphosphate finished product. The corn soaking water is used as the raw material for extracting the inositol triphosphate, so that the production cost is low, the process is simple, the operation is simple and convenient, the method is suitable for industrial production, and meanwhile, the obtained inositol triphosphate is easy to separate, and the purity of the product is high.
Description
Technical Field
The utility model relates to the technical field of corn steep water backwater utilization, in particular to a device for preparing inositol triphosphate by using corn steep water.
Background
Inositol phosphates include inositol 1-phosphate [ inosite-1-phosphate, ins 1-P]1,4-bisphosphate inositol 1, 4-biphosphate, ins 1- (1, 4) P2]And 1,4, 5-triphosphoinositol-1, 4, 5-triphosphonates, IP3, etc. They are derived in vivo from the enzymatic hydrolysis of phosphatidylinositol species (e.g., phospholipase C). Nearly 20 different phosphoinositides have been found in cells to date, of which many play an important role as information substances. Most important is inositol triphosphate (IP 3), which is the enzymatic hydrolysate of phosphatidylinositol triphosphate. Its main function is to induce Ca 2+ Released from intracellular stores, and instantaneously increases Ca in cytosol 2+ Concentration. Because this process is based on Ca 2+ Is a widely existing intracellular messenger substance, so this enables the important regulatory action of cellular responses, and it has a complementary relationship with the regulatory action of diacylglycerol (diacylglycerol), mainly used as biochemical and medical agents.
Yu Yigang et al ("high activity phytase method for inositol triphosphate", grain and feed industry, 1999, 03) studied a process for hydrolyzing sodium phytate by using high activity Novo phytase (EC.3.1.3.8), separating and obtaining pure inositol triphosphate and inositol tetraphosphate by using ion exchange resin, wherein the phytase has severe preservation and reaction conditions, improves the production cost, and the yield of the product is directly affected by the activity of phytase, has poor process stability, is not easy to separate inositol triphosphate and inositol tetraphosphate, and has poor purity of the product.
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 preparing inositol triphosphate by using corn soaking water is good in process stability, low in production cost and high in product purity.
In order to solve the technical problems, the technical scheme of the utility model is as follows:
the utility model provides an utilize device of maize steeping water preparation inositol triphosphate, includes maize steeping water jar, maize steeping water jar's export is through the pipeline intercommunication to anion exchange resin column's lower extreme entry, anion exchange resin column upper end export is through the pipeline intercommunication there is the temporary storage jar, anion exchange resin column's upper end entry is through the pipeline intercommunication there is the analytical solution jar, anion exchange resin column's lower extreme export is through the pipeline intercommunication there is the analytical solution jar, the export of analytical solution jar is through the pipeline intercommunication there is the hydrolysis tank, the entry of hydrolysis tank is through the pipeline intercommunication there is the catalyst jar, the export of hydrolysis tank is through the pipeline intercommunication there is first filter, the filtrate export of first filter is through the pipeline intercommunication there is first concentrator, the export of first concentrator is through the pipeline intercommunication there is concentrate jar, the export of concentrate jar is through the pipeline intercommunication there is the simulated moving bed, the inositol triphosphate solution jar that the simulated moving bed is through the pipeline intercommunication there is the inositol triphosphate solution jar, the phosphoric acid phase export of simulated moving bed is through the pipeline intercommunication to dilute phosphoric acid solution jar;
the outlet of the inositol triphosphate solution tank is communicated with a second concentrator through a pipeline, the outlet of the second concentrator is communicated with a second filter through a pipeline, the outlet of filtrate of the second filter is communicated with a crystallization tank through a pipeline, the outlet of the crystallization tank is communicated with a centrifugal machine through a pipeline, the solid phase outlet of the centrifugal machine is communicated with a dryer, and the outlet of the dryer is communicated with an inositol triphosphate finished product tank.
As an improved technical scheme, an upper end inlet and a lower end inlet of the anion exchange resin column are respectively communicated with a purified water tank through pipelines, and an upper end outlet and a lower end outlet of the anion exchange resin column are respectively communicated with a flushing water tank through pipelines.
As an improved technical scheme, the outlet of the flushing water tank is communicated with a first nanofiltration membrane device through a pipeline, the outlet of the first nanofiltration membrane device is communicated with the inlet of the purified water tank through a pipeline, and the molecular weight cut-off of the first nanofiltration membrane device is 150-200 MWCO.
As an improved technical scheme, an outlet of the analysis liquid tank is communicated with a second nanofiltration membrane device through a pipeline, a concentrated liquid outlet of the second nanofiltration membrane device is communicated to the hydrolysis tank through a pipeline, and the molecular weight cut-off of the second nanofiltration membrane device is 300-400 MWCO.
As an improved technical scheme, a clear liquid outlet of the second nanofiltration membrane device is communicated with a resolving agent preparation tank through a pipeline, and an outlet of the resolving agent preparation tank is communicated with the resolving agent tank through a pipeline.
As an improved technical scheme, the second filter is an activated carbon filter.
As a preferable technical scheme, the liquid phase outlet of the centrifugal machine is communicated with the crystallization tank through a pipeline.
As the preferable technical scheme, the outlet of the dilute phosphoric acid solution tank is communicated with a distillation kettle through a pipeline, and the outlet of the distillation kettle is communicated with a phosphoric acid 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 device for preparing inositol triphosphate by using corn soaking water, which comprises a corn soaking water tank, wherein an outlet of the corn soaking water tank is communicated with a lower end inlet of an anion exchange resin column through a pipeline, an upper end outlet of the anion exchange resin column is communicated with a temporary storage tank through a pipeline, an upper end inlet of the anion exchange resin column is communicated with a resolving agent tank through a pipeline, a lower end outlet of the anion exchange resin column is communicated with a resolving liquid tank through a pipeline, an outlet of the resolving liquid tank is communicated with a hydrolysis tank through a pipeline, an inlet of the hydrolysis tank is communicated with a catalyst tank through a pipeline, an outlet of the hydrolysis tank is communicated with a first filter through a pipeline, a filtrate outlet of the first filter is communicated with a first concentrator through a pipeline, an outlet of the first concentrator is communicated with a concentrate tank through a pipeline, an outlet of the concentrate tank is communicated with a simulated moving bed through a pipeline, an inositol triphosphate phase outlet of the simulated moving bed is communicated with an inositol triphosphate solution tank through a pipeline, and a phosphoric acid phase outlet of the simulated moving bed is communicated with a dilute phosphoric acid solution tank through a pipeline; the outlet of the inositol triphosphate solution tank is communicated with a second concentrator through a pipeline, the outlet of the second concentrator is communicated with a second filter through a pipeline, the outlet of filtrate of the second filter is communicated with a crystallization tank through a pipeline, the outlet of the crystallization tank is communicated with a centrifugal machine through a pipeline, the solid phase outlet of the centrifugal machine is communicated with a dryer, and the outlet of the dryer is communicated with an inositol triphosphate finished product tank. The corn soaking water enters an anion exchange resin column to adsorb phytic acid, and the adsorbed corn water enters a temporary storage tank and finally is transferred to a starch factory for reprocessing. The analytical agent in the analytical agent tank enters an anion exchange resin column to analyze the analytical agent, the obtained analytical solution enters a hydrolysis tank, inositol triphosphate is generated under the action of a catalyst, a solid catalyst and insoluble impurities are removed through a first filter, filtrate enters a first concentrator, concentrated solution enters a simulated moving bed to be separated, and inositol triphosphate solution and dilute phosphoric acid solution are obtained, wherein the inositol triphosphate solution is filtered again after being concentrated by a second concentrator, and filtrate is crystallized, centrifuged and dried to obtain an inositol triphosphate finished product. The corn soaking water is used as the raw material for extracting the inositol triphosphate, so that the production cost is low, the process is simple, the operation is simple and convenient, the method is suitable for industrial production, and meanwhile, the obtained inositol triphosphate is easy to separate, and the purity of the product is high.
The upper end inlet and the lower end inlet of the anion exchange resin column are respectively communicated with a purified water tank through pipelines, and the upper end outlet and the lower end outlet of the anion exchange resin column are respectively communicated with a flushing water tank through pipelines. The anion exchange resin column is washed by purified water, so that most of impurities such as proteins, calcium, magnesium and the like are removed, the post-treatment difficulty is reduced, and the purity of the product is improved.
The outlet of the flushing water tank is communicated with a first nanofiltration membrane device through a pipeline, the outlet of the first nanofiltration membrane device is communicated with the inlet of the purification water tank through a pipeline, and the molecular weight cut-off of the first nanofiltration membrane device is 150-200 MWCO. The washing water is treated by the first nanofiltration membrane device, and the obtained treated water can be reused for washing the anion exchange resin column, so that the production cost is reduced, and the economic benefit is improved.
The outlet of the analysis liquid tank is communicated with a second nanofiltration membrane device through a pipeline, the concentrated liquid outlet of the second nanofiltration membrane device is communicated to the hydrolysis tank through a pipeline, and the molecular weight cut-off of the second nanofiltration membrane device is 300-400 MWCO. The second nanofiltration membrane device is used for concentrating the analysis liquid, so that impurities in the analysis liquid are further removed, the subsequent concentration time of the first concentrator is shortened, the process period is shortened, and the cost is saved.
The clear liquid outlet of the second nanofiltration membrane device is communicated with a resolving agent preparation tank through a pipeline, and the outlet of the resolving agent preparation tank is communicated to the resolving agent tank through a pipeline. The clear liquid of the second nanofiltration membrane device can be used for preparing the resolving agent again, so that the trouble of post-treatment is eliminated, and meanwhile, the cost is saved.
The second filter is an activated carbon filter, the materials in the second concentrator are decolorized through the second filter, the purity and chromaticity of inositol triphosphate are good, and the quality of products is improved.
The liquid phase outlet of the centrifugal machine is communicated to the crystallization tank through a pipeline, and the centrifugal mother liquor is sleeved, so that the waste of raw materials is avoided, the yield of products is improved, and the trouble of mother liquor treatment is avoided.
The outlet of the dilute phosphoric acid solution tank is communicated with a distillation kettle through a pipeline, the outlet of the distillation kettle is communicated with a phosphoric acid tank through a pipeline, and the dilute phosphoric acid solution is distilled and dehydrated to obtain a high-concentration phosphoric acid solution, so that the economic benefit is higher, and meanwhile, the requirements of different customers can be met.
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. corn soaking water tank; 2. an anion exchange resin column; 3. a temporary storage tank; 4. a resolving agent tank; 5. resolving a liquid tank; 6. a hydrolysis tank; 7. a catalyst tank; 8. a first filter; 9. a first concentrator; 10. a concentrate tank; 11. a simulated moving bed; 12. inositol triphosphate solution tank; 13. dilute phosphoric acid solution tank; 14. a second concentrator; 15. a second filter; 16. a crystallization tank; 17. a centrifuge; 18. a dryer; 19. a inositol triphosphate finished product tank; 20. a purified water tank; 21. flushing the water tank; 22. a first nanofiltration membrane device; 23. a second nanofiltration membrane device; 24. a resolving agent preparation tank; 25. a distillation still; 26. a phosphoric acid tank.
Detailed Description
The utility model is further illustrated in the following, in conjunction with the accompanying drawings and examples.
As shown in fig. 1, the device for preparing inositol triphosphate by using corn steep water comprises a corn steep water tank 1, wherein an outlet of the corn steep water tank 1 is communicated with a lower end inlet of an anion exchange resin column 2 through a pipeline, an upper end outlet of the anion exchange resin column 2 is communicated with a temporary storage tank 3 through a pipeline, an upper end inlet of the anion exchange resin column 2 is communicated with a resolving agent tank 4 through a pipeline, a hydrochloric acid solution is selected as resolving agent in the embodiment, a lower end outlet of the anion exchange resin column 2 is communicated with a resolving liquid tank 5 through a pipeline, an outlet of the resolving liquid tank 5 is communicated with a hydrolysis tank 6 through a pipeline, an inlet of the hydrolysis tank 6 is communicated with a catalyst tank 7 through a pipeline, an outlet of the hydrolysis tank 6 is communicated with a first filter 8 through a pipeline, a filtrate outlet of the first filter 8 is communicated with a first concentrator 9 through a pipeline, an outlet of the first concentrator 9 is communicated with a concentrating liquid tank 10 through a pipeline, an outlet of the concentrating liquid tank 10 is communicated with a simulated moving bed 11, an inositol triphosphate outlet of the simulated moving bed 11 is communicated with an inositol triphosphate liquid tank 12 through a simulated moving bed 13; the outlet of the inositol triphosphate solution tank 12 is communicated with a second concentrator 14 through a pipeline, the outlet of the second concentrator 14 is communicated with a second filter 15 through a pipeline, the filtrate outlet of the second filter 15 is communicated with a crystallization tank 16 through a pipeline, the outlet of the crystallization tank 16 is communicated with a centrifugal machine 17 through a pipeline, the solid phase outlet of the centrifugal machine 17 is communicated with a dryer 18, and the outlet of the dryer 18 is communicated with an inositol triphosphate finished product tank 19. The corn soaking water enters an anion exchange resin column 2 to adsorb phytic acid, and the adsorbed corn water enters a temporary storage tank 3 and finally is transferred to a starch factory for reprocessing, so that the economic benefit is improved. The resolving agent in the resolving agent tank 4 enters the anion exchange resin column 2 to resolve the resolving agent, the obtained resolving solution enters the hydrolysis tank 6, inositol triphosphate is generated under the action of a catalyst, zirconium sulfate is selected as the catalyst in the embodiment, after hydrolysis is completed, solid superacid and phytic acid hydrolysis system can be separated only by filtration, difficulty in separation and impurity removal of phytic acid hydrolysis products is avoided, the solid catalyst and insoluble impurities are removed through the first filter 8, filtrate enters the first concentrator 9, concentrated solution enters the simulated moving bed 11 to separate, inositol triphosphate solution and dilute phosphoric acid solution are obtained, wherein the inositol triphosphate solution is filtered again after being concentrated by the second concentrator 14, and the filtrate is crystallized, centrifuged and dried, so that inositol triphosphate finished product is obtained. The corn soaking water is used as the raw material for extracting the inositol triphosphate, so that the production cost is low, the process is simple, the operation is simple and convenient, the method is suitable for industrial production, and meanwhile, the obtained inositol triphosphate is easy to separate, and the purity of the product is high.
The upper inlet and the lower inlet of the anion exchange resin column 2 are respectively communicated with a purified water tank 20 through pipelines, and the upper outlet and the lower outlet of the anion exchange resin column 2 are respectively communicated with a flushing water tank 21 through pipelines. The anion exchange resin column 2 is washed by purified water, so that most of impurities such as proteins, calcium, magnesium and the like are removed, the post-treatment difficulty is reduced, and the purity of the product is improved.
The outlet of the flushing water tank 21 is communicated with a first nanofiltration membrane device 22 through a pipeline, the outlet of the first nanofiltration membrane device 22 is communicated with the inlet of the purified water tank 20 through a pipeline, and the molecular weight cut-off of the first nanofiltration membrane device 22 is 150-200 MWCO. The washing water is treated by the first nanofiltration membrane device 22, and the obtained treated water can be reused for washing the anion exchange resin column 2, so that the production cost is reduced, and the economic benefit is improved.
The outlet of the analysis liquid tank 5 is communicated with a second nanofiltration membrane device 23 through a pipeline, the concentrated liquid outlet of the second nanofiltration membrane device 23 is communicated to the hydrolysis tank 6 through a pipeline, and the molecular weight cut-off of the second nanofiltration membrane device 23 is 300-400 MWCO. The second nanofiltration membrane device 23 is used for concentrating the analysis liquid, so that impurities in the analysis liquid are further removed, the subsequent concentration time of the first concentrator 9 is shortened, the process period is shortened, and the cost is saved.
The clear liquid outlet of the second nanofiltration membrane device 23 is communicated with a resolving agent preparation tank 24 through a pipeline, and the outlet of the resolving agent preparation tank 24 is communicated with the resolving agent tank 4 through a pipeline. The clear liquid of the second nanofiltration membrane device 23 can be used for preparing the resolving agent again, so that the trouble of post-treatment is eliminated, and meanwhile, the cost is saved.
The second filter 15 is an activated carbon filter, the materials in the second concentrator 14 are decolorized through the second filter 15, the purity and chromaticity of inositol triphosphate are good, and the quality of the product is improved.
The liquid phase outlet of the centrifugal machine 17 is communicated to the crystallization tank 16 through a pipeline, and the centrifugal mother liquor is sleeved, so that the waste of raw materials is avoided, the yield of products is improved, and the trouble of mother liquor treatment is avoided.
The outlet of the dilute phosphoric acid solution tank 13 is communicated with a distillation kettle 25 through a pipeline, the outlet of the distillation kettle 25 is communicated with a phosphoric acid tank 26 through a pipeline, and the dilute phosphoric acid solution is distilled and dehydrated to obtain a high-concentration phosphoric acid solution, so that the economic benefit is higher, and meanwhile, the requirements of different customers can be met.
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. Further, it is understood that various changes and modifications may be made by those 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 claims appended hereto.
Claims (8)
1. The utility model provides an utilize device of maize steeping water preparation inositol triphosphate, includes the maize steeping water jar, the export of maize steeping water jar is through the lower extreme entry of pipeline intercommunication to anion exchange resin post, anion exchange resin post upper end export has the jar of keeping in through the pipeline intercommunication, the upper end entry of anion exchange resin post has the analytical agent jar through the pipeline intercommunication, the lower extreme export of anion exchange resin post has the analytical fluid reservoir through the pipeline intercommunication, its characterized in that: the outlet of the analysis liquid tank is communicated with a hydrolysis tank through a pipeline, the inlet of the hydrolysis tank is communicated with a catalyst tank through a pipeline, the outlet of the hydrolysis tank is communicated with a first filter through a pipeline, the filtrate outlet of the first filter is communicated with a first concentrator through a pipeline, the outlet of the first concentrator is communicated with a concentrated liquid tank through a pipeline, the outlet of the concentrated liquid tank is communicated with a simulated moving bed through a pipeline, the inositol triphosphate phase outlet of the simulated moving bed is communicated with an inositol triphosphate solution tank through a pipeline, and the phosphoric acid phase outlet of the simulated moving bed is communicated with a dilute phosphoric acid solution tank through a pipeline;
the outlet of the inositol triphosphate solution tank is communicated with a second concentrator through a pipeline, the outlet of the second concentrator is communicated with a second filter through a pipeline, the outlet of filtrate of the second filter is communicated with a crystallization tank through a pipeline, the outlet of the crystallization tank is communicated with a centrifugal machine through a pipeline, the solid phase outlet of the centrifugal machine is communicated with a dryer, and the outlet of the dryer is communicated with an inositol triphosphate finished product tank.
2. An apparatus for preparing inositol triphosphate from corn steep water as set forth in claim 1, wherein: the upper end inlet and the lower end inlet of the anion exchange resin column are respectively communicated with a purified water tank through pipelines, and the upper end outlet and the lower end outlet of the anion exchange resin column are respectively communicated with a flushing water tank through pipelines.
3. An apparatus for preparing inositol triphosphate from corn steep water as set forth in claim 2, wherein: the outlet of the flushing water tank is communicated with a first nanofiltration membrane device through a pipeline, the outlet of the first nanofiltration membrane device is communicated with the inlet of the purification water tank through a pipeline, and the molecular weight cut-off of the first nanofiltration membrane device is 150-200 MWCO.
4. An apparatus for preparing inositol triphosphate from corn steep water as set forth in claim 1, wherein: the outlet of the analysis liquid tank is communicated with a second nanofiltration membrane device through a pipeline, the concentrated liquid outlet of the second nanofiltration membrane device is communicated to the hydrolysis tank through a pipeline, and the molecular weight cut-off of the second nanofiltration membrane device is 300-400 MWCO.
5. An apparatus for preparing inositol triphosphate from corn steep water as set forth in claim 4, wherein: the clear liquid outlet of the second nanofiltration membrane device is communicated with a resolving agent preparation tank through a pipeline, and the outlet of the resolving agent preparation tank is communicated to the resolving agent tank through a pipeline.
6. An apparatus for preparing inositol triphosphate from corn steep water as set forth in claim 1, wherein: the second filter is an activated carbon filter.
7. An apparatus for preparing inositol triphosphate from corn steep water as set forth in claim 1, wherein: and a liquid phase outlet of the centrifugal machine is communicated to the crystallization tank through a pipeline.
8. An apparatus for preparing inositol triphosphate from corn steep water as set forth in claim 1, wherein: the outlet of the dilute phosphoric acid solution tank is communicated with a distillation kettle through a pipeline, and the outlet of the distillation kettle is communicated with a phosphoric acid tank through a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322302914.0U CN220657493U (en) | 2023-08-24 | 2023-08-24 | Device for preparing inositol triphosphate by using corn soaking water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322302914.0U CN220657493U (en) | 2023-08-24 | 2023-08-24 | Device for preparing inositol triphosphate by using corn soaking water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220657493U true CN220657493U (en) | 2024-03-26 |
Family
ID=90342151
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322302914.0U Active CN220657493U (en) | 2023-08-24 | 2023-08-24 | Device for preparing inositol triphosphate by using corn soaking water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220657493U (en) |
-
2023
- 2023-08-24 CN CN202322302914.0U patent/CN220657493U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100422347C (en) | Crystalline glucose producing process based on whole membrane method | |
| CN101863822B (en) | Production method for extracting tryptophan from fermentation liquor by one-step refining | |
| CN108822163B (en) | Comprehensive cyclic production method of D-glucosamine hydrochloride | |
| CN104529755B (en) | A kind of method being separated α-ketoglutaric acid from conversion fluid | |
| CN109265498B (en) | Method for preparing N-acetylneuraminic acid by integrated separation and purification of polysialic acid | |
| CN108779147B (en) | Reduced glutathione crystal and method for producing same | |
| CN112979482B (en) | High-purity L-valine as well as preparation method and application thereof | |
| CN108276292A (en) | A kind of separation method of 1,5- pentanediamines | |
| CN106831894A (en) | A kind of method that deacetylation Coupling Adsorption separates D aminoglucose hydrochlorides | |
| CN116813447A (en) | Method for co-producing inositol and disodium hydrogen phosphate by using corn soaking water | |
| CN103709235A (en) | Method for reducing solvent use amount and extracting high-purity enramycin | |
| CN220657493U (en) | Device for preparing inositol triphosphate by using corn soaking water | |
| CN111171097A (en) | Separation and purification method for producing adenosine by fermentation | |
| CN101100437B (en) | Method for preparing high-purity beta-alanine | |
| CN109369731B (en) | Method for removing glucose in xylose production process | |
| CN113735136B (en) | Process method for preparing potassium salt and byproduct magnesium salt by using corn soaking water | |
| EP4214326A2 (en) | Continuous ion exchange and esterification of fermented malonic acid | |
| CN103570573B (en) | Method for extracting alpha-aminoadipic acid from enzymatic waste liquor | |
| EP1330533A2 (en) | Method of preparing a modified corn steep liquor product | |
| CN220846152U (en) | Device for producing D-chiral inositol and glucuronic acid by utilizing inositol | |
| CN108220351B (en) | Method for preparing L-arginine-alpha-ketoglutaric acid by biological enzyme method | |
| CN219615074U (en) | Inositol apparatus for producing | |
| CN219218037U (en) | Device for extracting myoethanol and monopotassium phosphate from corn soaking water | |
| CN220788620U (en) | Device for producing scyllo-inositol by using inositol solution | |
| CN114436816B (en) | Method for efficiently extracting shikimic acid by ion exchange technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |