CN219784729U - Iron phytate recovery unit and device of production inositol and ferric phosphate that uses it - Google Patents
Iron phytate recovery unit and device of production inositol and ferric phosphate that uses it Download PDFInfo
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- CN219784729U CN219784729U CN202320457438.7U CN202320457438U CN219784729U CN 219784729 U CN219784729 U CN 219784729U CN 202320457438 U CN202320457438 U CN 202320457438U CN 219784729 U CN219784729 U CN 219784729U
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 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 title claims abstract description 64
- 235000002949 phytic acid Nutrition 0.000 title claims abstract description 64
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 42
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 title claims abstract description 33
- CDAISMWEOUEBRE-UHFFFAOYSA-N scyllo-inosotol Natural products OC1C(O)C(O)C(O)C(O)C1O CDAISMWEOUEBRE-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 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 title claims abstract description 25
- 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 title claims abstract description 25
- 229960000367 inositol Drugs 0.000 title claims abstract description 25
- 238000011084 recovery Methods 0.000 title claims abstract description 22
- 229910000399 iron(III) phosphate Inorganic materials 0.000 title abstract description 24
- 239000005955 Ferric phosphate Substances 0.000 title abstract description 23
- 229940032958 ferric phosphate Drugs 0.000 title abstract description 23
- 238000004519 manufacturing process Methods 0.000 title description 4
- 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 73
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 73
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 71
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 71
- 239000007788 liquid Substances 0.000 claims abstract description 56
- 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 claims abstract description 50
- 240000008042 Zea mays Species 0.000 claims abstract description 50
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 claims abstract description 50
- 235000002017 Zea mays subsp mays Nutrition 0.000 claims abstract description 50
- 235000005822 corn Nutrition 0.000 claims abstract description 50
- 239000000467 phytic acid Substances 0.000 claims abstract description 50
- 229940068041 phytic acid Drugs 0.000 claims abstract description 50
- 239000000463 material Substances 0.000 claims abstract description 38
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 238000002791 soaking Methods 0.000 claims abstract description 32
- 239000000243 solution Substances 0.000 claims abstract description 25
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 20
- 239000012266 salt solution Substances 0.000 claims abstract description 18
- 150000003841 chloride salts Chemical class 0.000 claims abstract description 15
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims abstract description 11
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims abstract description 11
- 238000005406 washing Methods 0.000 claims description 30
- 239000007791 liquid phase Substances 0.000 claims description 15
- 239000000919 ceramic Substances 0.000 claims description 14
- 239000000706 filtrate Substances 0.000 claims description 14
- 238000002425 crystallisation Methods 0.000 claims description 13
- 230000008025 crystallization Effects 0.000 claims description 13
- 239000012528 membrane Substances 0.000 claims description 13
- 238000004062 sedimentation Methods 0.000 claims description 13
- 230000007062 hydrolysis Effects 0.000 claims description 11
- 238000006460 hydrolysis reaction Methods 0.000 claims description 11
- 239000003957 anion exchange resin Substances 0.000 claims description 10
- 229910000398 iron phosphate Inorganic materials 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 9
- 239000012065 filter cake Substances 0.000 claims description 8
- 238000001953 recrystallisation Methods 0.000 claims description 8
- 239000007790 solid phase Substances 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 5
- 239000002367 phosphate rock Substances 0.000 abstract description 4
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 abstract description 4
- 230000003301 hydrolyzing effect Effects 0.000 abstract description 2
- 239000010865 sewage Substances 0.000 abstract description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract 2
- 229910052799 carbon Inorganic materials 0.000 abstract 2
- 229920002472 Starch Polymers 0.000 abstract 1
- 230000007774 longterm Effects 0.000 abstract 1
- 238000006386 neutralization reaction Methods 0.000 abstract 1
- 235000019698 starch Nutrition 0.000 abstract 1
- 239000008107 starch Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 description 14
- 239000002994 raw material Substances 0.000 description 10
- 239000002699 waste material Substances 0.000 description 9
- 238000001556 precipitation Methods 0.000 description 8
- 238000004458 analytical method Methods 0.000 description 7
- 238000001914 filtration Methods 0.000 description 7
- 239000002244 precipitate Substances 0.000 description 7
- 238000003756 stirring Methods 0.000 description 7
- 150000001804 chlorine Chemical class 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 238000005342 ion exchange Methods 0.000 description 4
- 239000011259 mixed solution Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 241001465754 Metazoa Species 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N EtOH Substances CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 2
- LFVGISIMTYGQHF-UHFFFAOYSA-N ammonium dihydrogen phosphate Chemical compound [NH4+].OP(O)([O-])=O LFVGISIMTYGQHF-UHFFFAOYSA-N 0.000 description 2
- 229910000387 ammonium dihydrogen phosphate Inorganic materials 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 235000019837 monoammonium phosphate Nutrition 0.000 description 2
- 239000006012 monoammonium phosphate Substances 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 229920002261 Corn starch Polymers 0.000 description 1
- 239000005696 Diammonium phosphate Substances 0.000 description 1
- 208000004930 Fatty Liver Diseases 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 206010019708 Hepatic steatosis Diseases 0.000 description 1
- 208000035150 Hypercholesterolemia Diseases 0.000 description 1
- 239000005956 Metaldehyde Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 208000019425 cirrhosis of liver Diseases 0.000 description 1
- 239000008120 corn starch Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 1
- 229910000388 diammonium phosphate Inorganic materials 0.000 description 1
- 235000019838 diammonium phosphate Nutrition 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 208000010706 fatty liver disease Diseases 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 239000003102 growth factor Substances 0.000 description 1
- 208000006454 hepatitis Diseases 0.000 description 1
- 231100000283 hepatitis Toxicity 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- GELKBWJHTRAYNV-UHFFFAOYSA-K lithium iron phosphate Chemical compound [Li+].[Fe+2].[O-]P([O-])([O-])=O GELKBWJHTRAYNV-UHFFFAOYSA-K 0.000 description 1
- GKKDCARASOJPNG-UHFFFAOYSA-N metaldehyde Chemical compound CC1OC(C)OC(C)OC(C)O1 GKKDCARASOJPNG-UHFFFAOYSA-N 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003750 molluscacide Substances 0.000 description 1
- 230000002013 molluscicidal effect Effects 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 231100000240 steatosis hepatitis Toxicity 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Abstract
The utility model discloses a ferric phytate recovery device and a device for producing inositol and ferric phosphate by using the same, and relates to the technical field of corn soaking water recovery and utilization, wherein an ion exchange resin column is communicated with a corn soaking water pipeline, a feed inlet of the ion exchange resin column is respectively communicated with a resolving agent storage tank and a process water storage tank, and an outlet of the ion exchange resin column is communicated with a resolving liquid storage tank; the material outlet of the analytic liquid storage tank is communicated with a reaction kettle, the material inlet of the reaction kettle is respectively communicated with a hydrochloric acid storage tank and a ferric chloride solution storage tank, the reaction kettle is communicated with a first plate-and-frame filter press and a chloride salt solution tank, and the first plate-and-frame filter press is communicated to the phytic acid iron storage tank. And (3) recovering the phytic acid in the corn soaking water to obtain phytic acid iron, and then hydrolyzing, separating and purifying the phytic acid iron to obtain inositol and ferric phosphate products. Saving a great amount of phosphorite resources for the country, meeting the current national carbon emission and carbon neutralization trend, and simultaneously solving the long-term sewage emission problem in the starch industry.
Description
Technical Field
The utility model relates to the technical field of recycling of corn soaking water, in particular to an iron phytate recycling device and a device for producing inositol and ferric phosphate by using the same.
Background
Inositol is a substance widely present in foods and is structurally similar to glucose. Inositol is widely distributed in animals and plants, and is a growth factor of animals and microorganisms. Is mainly used for treating liver cirrhosis, hepatitis, fatty liver, hypercholesterolemia and the like.
Ferric phosphate, also known as ferric phosphate, ferric orthophosphate, is a white, off-white monoclinic crystal powder. The main application is to manufacture lithium iron phosphate battery materials, catalysts, ceramics and the like. Iron phosphate is also one of a few molluscicides approved for use in organic agriculture. Unlike metaldehyde used previously, it is non-toxic to pets and wild animals. In the current process route of ferric phosphate, phosphorus element is derived from phosphorite and is an indispensable resource of ferric phosphate, and phosphorite is positioned at the upstream of an iron phosphate industrial chain, and monoammonium phosphate, diammonium phosphate and high-purity phosphoric acid can be produced by a wet method or a thermal method; and (3) reacting the high-purity phosphoric acid with monoammonium phosphate, and adjusting the pH value to obtain the ferric phosphate.
Corn is a high phosphorus, potassium-rich plant, 1 ton of corn containing 3kg phosphorus, 3.2kg potassium. In the process of producing corn starch by wet processing corn, the produced corn steep water contains about 1% of phytic acid, iron phytate is prepared by separation and purification through an ion exchange technology, and inositol and iron phosphate products are prepared by chemical reaction and separation and purification.
Disclosure of Invention
The first technical problem to be solved by the utility model is as follows: aiming at the defects existing in the prior art, the device for recycling the phytic acid iron by using the corn soaking water is provided, the phytic acid in the corn soaking water is recycled, and the phytic acid iron is prepared through ion exchange and separation and purification, so that the waste of raw materials and the environmental pollution caused by sewage discharge are avoided.
In order to solve the first technical problem, the technical scheme of the utility model is as follows:
the device for recycling the phytic acid iron by using the corn soaking water comprises an ion exchange resin column, wherein an inlet of the ion exchange resin column is communicated with a corn soaking water pipeline, a feed inlet of the ion exchange resin column is respectively communicated with a resolving agent storage tank and a process water storage tank through pipelines, and an outlet of the ion exchange resin column is communicated with a resolving liquid storage tank through pipelines;
the material outlet of the analytic liquid storage tank is communicated with a reaction kettle through a pipeline, the material inlet of the reaction kettle is respectively communicated with a hydrochloric acid storage tank and a ferric chloride solution storage tank through pipelines, the outlet of the reaction kettle is respectively communicated with a first plate-and-frame filter press and a chloride solution tank through pipelines, and the solid phase outlet of the first plate-and-frame filter press is communicated to the phytic acid iron storage tank through a pipeline.
As an improved technical scheme, the inlet of the ion exchange resin column is communicated with a clarified liquid storage tank through a pipeline, the corn steep water pipeline is communicated with a sedimentation tank or a ceramic membrane, and the liquid phase outlet of the sedimentation tank or the ceramic membrane is communicated with the inlet of the clarified liquid storage tank through a pipeline.
As an improved technical scheme, the ion exchange resin column is an anion exchange resin column.
As an improved technical scheme, an outlet of the ion exchange resin column is communicated with an effluent liquid storage tank through a pipeline.
As an improved technical scheme, an outlet of the ion exchange resin column is communicated with a resolving agent recovery tank through a pipeline.
As an improved technical scheme, the liquid phase outlet of the first plate-and-frame filter press is communicated with the chloride salt solution tank through a pipeline.
As a preferable technical scheme, the chlorine salt solution tank is communicated with the resolving agent storage tank through a pipeline.
The second technical problem to be solved by the utility model is as follows: aiming at the defects existing in the prior art, the device for preparing the inositol and the ferric phosphate by using the corn soaking water to produce the inositol and the ferric phosphate through ion exchange, chemical reaction and separation and purification is provided, so that phosphorite resources are saved.
In order to solve the second technical problem, the technical scheme of the utility model is as follows:
the device for producing the myo-ethanol and the ferric phosphate by using the corn steep water comprises an ion exchange resin column, wherein an inlet of the ion exchange resin column is communicated with a corn steep water pipeline, a feed inlet of the ion exchange resin column is respectively communicated with a resolving agent storage tank and a process water storage tank through pipelines, and an outlet of the ion exchange resin column is communicated with a resolving liquid storage tank through pipelines;
the material outlet of the analytic liquid storage tank is communicated with a reaction kettle through a pipeline, the material inlet of the reaction kettle is respectively communicated with a hydrochloric acid storage tank and a ferric chloride solution storage tank through pipelines, the outlet of the reaction kettle is respectively communicated with a first plate-and-frame filter press and a chloride solution tank through pipelines, and the solid phase outlet of the first plate-and-frame filter press is communicated to the phytic acid iron storage tank through a pipeline;
the material outlet of the phytic acid iron storage tank is communicated with a hydrolysis kettle through a pipeline, the material outlet of the hydrolysis kettle is communicated with a second plate-and-frame filter press through a pipeline, the filtrate outlet of the second plate-and-frame filter press is communicated with a crystallization kettle through a pipeline, the material outlet of the crystallization kettle is communicated with a recrystallization kettle through a pipeline, and the material outlet of the recrystallization kettle is communicated with an inositol storage tank through a pipeline;
the filter cake outlet of the second plate-and-frame filter press is communicated to the washing kettle through a pipeline, the material outlet of the washing kettle is communicated to the third plate-and-frame filter press through a pipeline, the filter cake outlet of the third plate-and-frame filter press is communicated to the dryer through a pipeline, and the material outlet of the dryer is communicated to the iron phosphate storage tank through a pipeline.
As an improved technical scheme, the inlet of the ion exchange resin column is communicated with a clarified liquid storage tank through a pipeline, the corn steep water pipeline is communicated with a sedimentation tank or a ceramic membrane, and the liquid phase outlet of the sedimentation tank or the ceramic membrane is communicated with the inlet of the clarified liquid storage tank through a pipeline.
As an improved technical scheme, the ion exchange resin column is an anion exchange resin column.
As an improved technical scheme, an outlet of the ion exchange resin column is communicated with an effluent liquid storage tank through a pipeline.
As an improved technical scheme, an outlet of the ion exchange resin column is communicated with a resolving agent recovery tank through a pipeline.
As an improved technical scheme, the liquid phase outlet of the first plate-and-frame filter press is communicated with the chloride salt solution tank through a pipeline.
As a preferable technical scheme, the chlorine salt solution tank is communicated with the resolving agent storage tank through a pipeline.
As the preferable technical scheme, a filtrate outlet of the third plate-and-frame filter press is communicated with a material inlet of the crystallization kettle 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 recycling phytic acid iron by using corn soaking water, which comprises an ion exchange resin column, wherein an inlet of the ion exchange resin column is communicated with a corn soaking water pipeline, a feed inlet of the ion exchange resin column is respectively communicated with a resolving agent storage tank and a process water storage tank through pipelines, and an outlet of the ion exchange resin column is communicated with a resolving liquid storage tank through pipelines; the material outlet of the analytic liquid storage tank is communicated with a reaction kettle through a pipeline, the material inlet of the reaction kettle is respectively communicated with a hydrochloric acid storage tank and a ferric chloride solution storage tank through pipelines, the outlet of the reaction kettle is respectively communicated with a first plate-and-frame filter press and a chloride solution tank through pipelines, and the solid phase outlet of the first plate-and-frame filter press is communicated to the phytic acid iron storage tank through a pipeline. The corn soaking water enters an ion exchange resin column, then phytic acid is adsorbed, the saturated ion exchange column is adsorbed, the corn soaking water in the ion exchange resin column is replaced by water top washing, and then the phytic acid analysis solution is obtained after analysis by a resolving agent. The obtained phytic acid analysis solution is mixed with ferric chloride solution to carry out double decomposition precipitation reaction, and pH is regulated by hydrochloric acid to generate phytic acid ferric precipitate and chloride salt solution. Adding water into the phytic acid iron precipitate, stirring, washing and filtering to obtain a refined phytic acid iron product.
According to the utility model, the inlet of the ion exchange resin column is communicated with a clarified liquid storage tank through a pipeline, the corn steep water pipeline is communicated with a sedimentation tank or a ceramic membrane, and the liquid phase outlet of the sedimentation tank or the ceramic membrane is communicated with the inlet of the clarified liquid storage tank through a pipeline. Corn soaking water is treated by a sedimentation tank or a ceramic membrane to obtain clear filtrate, the ion exchange resin column is not easy to be blocked, and the purity of the obtained product is higher.
The outlet of the ion exchange resin column is communicated with an effluent liquid storage tank through a pipeline, the effluent liquid storage tank can recycle effluent liquid generated after corn soaking water enters the ion exchange resin column and effluent liquid generated by top washing of process water to replace corn soaking water in the ion exchange resin column, and phytic acid adsorption is carried out through the ion exchange resin column again, so that the waste of raw materials is reduced.
The outlet of the ion exchange resin column is communicated with the resolving agent recovery tank through a pipeline, the resolving agent remained inside the ion exchange resin column after the resolving is completed is subjected to top washing recovery through process water, and the resolving agent is reused for preparing and using the resolving agent, so that raw materials are fully utilized, and the cost is saved.
The liquid phase outlet of the first plate-and-frame filter press is communicated with the chlorine salt solution tank through a pipeline, and the effluent liquid of the liquid phase outlet of the first plate-and-frame filter press contains a certain amount of chlorine salt, is mixed with the chlorine salt solution generated by the precipitation reaction and is finally reused for preparing the resolving agent, so that raw materials are saved, and waste is greatly reduced.
The filtrate outlet of the third plate-and-frame filter press is communicated to the material inlet of the crystallization kettle through a pipeline, and effluent liquid of the filtrate outlet of the third plate-and-frame filter press contains a certain amount of inositol, and the inositol can be effectively recycled through crystallization and purification, so that waste is avoided.
Drawings
The utility model will be further described with reference to the drawings and examples.
FIG. 1 is a schematic structural view of embodiment 1 of the present utility model;
FIG. 2 is a schematic structural view of embodiment 2 of the present utility model;
wherein: 1. an ion exchange resin column; 2. corn soaking water pipeline; 3. a resolving agent storage tank; 4. a process water storage tank; 5. an analytical liquid storage tank; 6. a reaction kettle; 7. a hydrochloric acid storage tank; 8. an iron chloride solution storage tank; 9. a first plate and frame filter press; 10. chlorine salt solution tank; 11. a clarified liquid storage tank; 12. a sedimentation tank; 13. a ceramic membrane; 14. effluent liquid storage tank; 15. a resolving agent recovery tank; 16. a phytic acid iron storage tank; 17. a hydrolysis kettle; 18. a second plate and frame filter press; 19. a crystallization kettle; 20. a recrystallization kettle; 21. an inositol storage tank; 22. a washing kettle; 23. a third plate and frame filter press; 24. a dryer; 25. and a ferric phosphate storage tank.
Detailed Description
The utility model is further illustrated in the following, in conjunction with the accompanying drawings and examples.
Example 1
As shown in fig. 1, the device for recycling the phytic acid iron by using the corn steep water comprises an ion exchange resin column 1, wherein the ion exchange resin column 1 is an anion exchange resin column, an inlet of the ion exchange resin column 1 is communicated with a corn steep water pipeline 2, a feed inlet of the ion exchange resin column 1 is respectively communicated with a resolving agent storage tank 3 and a process water storage tank 4 through pipelines, and an outlet of the ion exchange resin column 1 is communicated with a resolving liquid storage tank 5 through pipelines; the material outlet of the analytic liquid storage tank 5 is communicated with a reaction kettle 6 through a pipeline, the material inlet of the reaction kettle 6 is respectively communicated with a hydrochloric acid storage tank 7 and an ferric chloride solution storage tank 8 through pipelines, the outlet of the reaction kettle 6 is respectively communicated with a first plate-and-frame filter press 9 and a chloride salt solution tank 10 through pipelines, and the solid phase outlet of the first plate-and-frame filter press 9 is communicated to a phytic acid iron storage tank 16 through a pipeline. The corn soaking water enters the ion exchange resin column 1, then phytic acid is adsorbed, the saturated ion exchange resin column 1 is adsorbed, the corn soaking water in the ion exchange resin column 1 is replaced by water top washing, and then the corn soaking water is resolved by a resolving agent to obtain phytic acid resolving liquid. The obtained phytic acid analysis solution is mixed with ferric chloride solution to carry out double decomposition precipitation reaction, and pH is regulated by hydrochloric acid to generate phytic acid ferric precipitate and chloride salt solution. Adding water into the phytic acid iron precipitate, stirring, washing and filtering to obtain a refined phytic acid iron product.
The inlet of the ion exchange resin column 1 is communicated with a clarified liquid storage tank 11 through a pipeline, the corn steep water pipeline 2 is communicated with a sedimentation tank 12, and the liquid phase outlet of the sedimentation tank 12 is communicated with the inlet of the clarified liquid storage tank 11 through a pipeline. Corn steep water is treated by the sedimentation tank 12 to obtain clear filtrate, the ion exchange resin column 1 is not easy to be blocked, and the purity of the obtained product is higher.
The outlet of the ion exchange resin column 1 is communicated with an effluent liquid storage tank 14 through a pipeline, the effluent liquid storage tank 14 can recycle effluent liquid generated after corn soaking water enters the ion exchange resin column 1 and effluent liquid generated by top washing of process water to replace the corn soaking water in the ion exchange resin column 1, and phytic acid adsorption is carried out through the ion exchange resin column 1 again, so that the waste of raw materials is reduced.
The outlet of the ion exchange resin column 1 is communicated with a resolving agent recovery tank 15 through a pipeline, resolving agent remained inside the ion exchange resin column 1 after resolving is recovered by top washing through process water, and the resolving agent is reused for preparing and using the resolving agent, so that raw materials are fully utilized, the cost is saved, and meanwhile, the environmental pollution is avoided.
The liquid phase outlet of the first plate-and-frame filter press 9 is communicated to the chloride salt solution tank 10 through a pipeline, and the effluent liquid of the liquid phase outlet of the first plate-and-frame filter press 9 contains a certain amount of chloride salt, is mixed with the chloride salt solution generated by the precipitation reaction and is finally reused for preparing and using the resolving agent, so that raw materials are saved, and waste is greatly reduced.
Example 2
As shown in fig. 2, the device for producing the myo-ethanol and the ferric phosphate by using the corn steep water comprises an ion exchange resin column 1, wherein the ion exchange resin column 1 is an anion exchange resin column, an inlet of the ion exchange resin column 1 is communicated with a corn steep water pipeline 2, a feed inlet of the ion exchange resin column 1 is respectively communicated with a resolving agent storage tank 3 and a process water storage tank 4 through pipelines, and an outlet of the ion exchange resin column 1 is communicated with a resolving liquid storage tank 5 through pipelines; the material outlet of the analytic liquid storage tank 5 is communicated with a reaction kettle 6 through a pipeline, the material inlet of the reaction kettle 6 is respectively communicated with a hydrochloric acid storage tank 7 and an ferric chloride solution storage tank 8 through pipelines, the outlet of the reaction kettle 6 is respectively communicated with a first plate-and-frame filter press 9 and a chloride solution tank 10 through pipelines, and the solid phase outlet of the first plate-and-frame filter press 9 is communicated to a phytic acid iron storage tank 16 through a pipeline; the material outlet of the phytic acid iron storage tank 16 is communicated with a hydrolysis kettle 17 through a pipeline, the material outlet of the hydrolysis kettle 17 is communicated to a second plate-and-frame filter press 18 through a pipeline, the filtrate outlet of the second plate-and-frame filter press 18 is communicated to a crystallization kettle 19 through a pipeline, the material outlet of the crystallization kettle 19 is communicated to a recrystallization kettle 20 through a pipeline, and the material outlet of the recrystallization kettle 20 is communicated to an inositol storage tank 21 through a pipeline; the filter cake outlet of the second plate-and-frame filter press 18 is communicated to the washing kettle 22 through a pipeline, the material outlet of the washing kettle 22 is communicated to the third plate-and-frame filter press 23 through a pipeline, the filter cake outlet of the third plate-and-frame filter press 23 is communicated to the dryer 24 through a pipeline, and the material outlet of the dryer 24 is communicated to the iron phosphate storage tank 25 through a pipeline. The corn soaking water enters the ion exchange resin column 1, then phytic acid is adsorbed, the saturated ion exchange resin column 1 is subjected to water top washing to replace the corn soaking water in the interior, and then the corn soaking water is resolved by a resolving agent to obtain phytic acid resolving liquid. The obtained phytic acid analysis solution is mixed with ferric chloride solution to carry out double decomposition precipitation reaction, and pH is regulated by hydrochloric acid to generate phytic acid ferric precipitate and chloride salt solution. Adding water into the phytic acid iron precipitate, stirring, washing and filtering to obtain a refined phytic acid iron product. The phytic acid iron and water are uniformly mixed and hydrolyzed in a hydrolysis kettle 17 to obtain ferric phosphate and inositol mixed solution, the ferric phosphate and inositol mixed solution is separated by a second plate-and-frame filter press 18, filter cakes and water enter a washing kettle 22, stirring and washing are carried out, filtration is carried out to obtain a ferric phosphate wet product, and the ferric phosphate wet product is obtained after drying; the filtrate and the washing liquid are inositol liquid, and the inositol finished product is obtained through concentrating crystallization and recrystallization.
The inlet of the ion exchange resin column 1 is communicated with a clarified liquid storage tank 11 through a pipeline, the corn steep water pipeline 2 is communicated with a ceramic membrane 13, and the liquid phase outlet of the ceramic membrane 13 is communicated with the inlet of the clarified liquid storage tank 11 through a pipeline. The corn steep water is treated by the ceramic membrane 13 to obtain clear filtrate, the ion exchange resin column 1 is not easy to be blocked, and the purity of the obtained product is higher.
The outlet of the ion exchange resin column 1 is communicated with an effluent liquid storage tank 14 through a pipeline, the effluent liquid storage tank 14 can recycle effluent liquid generated after corn soaking water enters the ion exchange resin column 1 and effluent liquid generated by top washing of process water to replace the corn soaking water in the ion exchange resin column 1, and phytic acid adsorption is carried out through the ion exchange resin column 1 again, so that the waste of raw materials is reduced.
The outlet of the ion exchange resin column 1 is communicated with a resolving agent recovery tank 15 through a pipeline, resolving agent remained in the ion exchange resin column 1 after resolving is completed is subjected to top washing recovery through process water, and the resolving agent is reused for preparing and using resolving agent, so that raw materials are fully utilized, and the cost is saved.
The liquid phase outlet of the first plate-and-frame filter press 9 is communicated to the chloride salt solution tank 10 through a pipeline, and the effluent liquid of the liquid phase outlet of the first plate-and-frame filter press 9 contains a certain amount of chloride salt, is mixed with the chloride salt solution generated by the precipitation reaction and is finally reused for preparing and using the resolving agent, so that raw materials are saved, and waste is greatly reduced.
The filtrate outlet of the third plate-and-frame filter press 23 is communicated to the material inlet of the hydrolysis kettle 17 through a pipeline, effluent liquid of the filtrate outlet of the third plate-and-frame filter press 23 contains a certain amount of inositol, and the inositol can be effectively recycled through crystallization and purification, so that waste is avoided.
The working principle of the utility model is as follows:
iron phytate recovery unit and use its apparatus of production inositol and ferric phosphate, specific operation steps are:
1) Adsorption: taking clarified corn soaking water, feeding the clarified corn soaking water into a 312 weak alkaline anion exchange resin column 1 to adsorb phytic acid, and feeding effluent into an effluent storage tank 14 for recycling.
2) Removing impurities: the saturated weak alkaline anion exchange resin column 1 is adsorbed, the corn soaking water in the weak alkaline anion exchange resin column is replaced by top washing of process water, and the effluent liquid after top washing replacement also enters an effluent liquid storage tank 14 for recycling.
3) Analysis: the purified weak alkaline anion exchange resin column 1 is resolved by sodium chloride solution as resolving agent to obtain phytic acid resolving liquid.
4) Washing: the resolved weak alkaline anion exchange resin column 1 is ejected out of the column resolving agent by process water, and the resolving agent replaced by top washing enters a resolving agent recovery tank 15.
5) Precipitation reaction: the obtained phytic acid analysis solution is mixed with ferric chloride solution to carry out double decomposition precipitation reaction, the pH value of hydrochloric acid is regulated to 1.0-1.5, and the reaction is carried out to generate phytic acid iron precipitate. And (3) precipitating the phytic acid iron, adding 2 times of water, stirring and washing, and filtering by a first plate-and-frame filter press 9 to obtain a refined phytic acid iron product.
6) And (3) mixing and stirring the iron phytate and water in the step (5) according to the proportion of 1:2, transferring the mixture into a hydrolysis kettle 17, and hydrolyzing for 10 hours at 160-190 ℃ under the condition of 0.6-0.8 Mpa to obtain the iron phosphate and inositol mixed solution.
7) Filtering the mixed solution of ferric phosphate and inositol by a second plate-and-frame filter press 18, putting a filter cake and pure water into a washing kettle 22 according to the ratio of 1:2, stirring and washing, filtering by a third plate-and-frame filter press 23 to obtain a wet ferric phosphate product, and drying to obtain a ferric phosphate product; the filtrate and the washing solution (effluent of the third plate-and-frame filter press 23) are inositol solution, and the inositol product is obtained by concentrating, crystallizing and recrystallizing.
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. Iron phytate recovery unit, its characterized in that: the corn soaking device comprises an ion exchange resin column, wherein an inlet of the ion exchange resin column is communicated with a corn soaking water pipeline, a feed inlet of the ion exchange resin column is respectively communicated with a resolving agent storage tank and a process water storage tank through pipelines, and an outlet of the ion exchange resin column is communicated with a resolving liquid storage tank through a pipeline;
the material outlet of the analytic liquid storage tank is communicated with a reaction kettle through a pipeline, the material inlet of the reaction kettle is respectively communicated with a hydrochloric acid storage tank and a ferric chloride solution storage tank through pipelines, the outlet of the reaction kettle is respectively communicated with a first plate-and-frame filter press and a chloride solution tank through pipelines, and the solid phase outlet of the first plate-and-frame filter press is communicated to the phytic acid iron storage tank through a pipeline.
2. An iron phytate recovery device as claimed in claim 1, characterized in that: the inlet of the ion exchange resin column is communicated with a clarified liquid storage tank through a pipeline, the corn steep water pipeline is communicated with a sedimentation tank or a ceramic membrane, and the liquid phase outlet of the sedimentation tank or the ceramic membrane is communicated with the inlet of the clarified liquid storage tank through a pipeline.
3. An iron phytate recovery device as claimed in claim 1, characterized in that: the ion exchange resin column is an anion exchange resin column.
4. An iron phytate recovery device as claimed in claim 1, characterized in that: the outlet of the ion exchange resin column is communicated with an effluent liquid storage tank through a pipeline.
5. An iron phytate recovery device as claimed in claim 1, characterized in that: and the outlet of the ion exchange resin column is communicated with a resolving agent recovery tank through a pipeline.
6. An iron phytate recovery device as claimed in claim 1, characterized in that: and a liquid phase outlet of the first plate-and-frame filter press is communicated with the chloride salt solution tank through a pipeline.
7. An iron phytate recovery device as claimed in claim 1, characterized in that: the chloride salt solution tank is communicated to the resolving agent storage tank through a pipeline.
8. An apparatus for producing inositol and iron phosphate, characterized in that: a material outlet of the phytic acid iron recycling device comprises a hydrolysis kettle, wherein the material outlet of the phytic acid iron storage tank is communicated with the hydrolysis kettle through a pipeline, the material outlet of the hydrolysis kettle is communicated with a second plate-and-frame filter press through a pipeline, a filtrate outlet of the second plate-and-frame filter press is communicated with a crystallization kettle through a pipeline, the material outlet of the crystallization kettle is communicated with a recrystallization kettle through a pipeline, and the material outlet of the recrystallization kettle is communicated with an inositol storage tank through a pipeline;
the filter cake outlet of the second plate-and-frame filter press is communicated to the washing kettle through a pipeline, the material outlet of the washing kettle is communicated to the third plate-and-frame filter press through a pipeline, the filter cake outlet of the third plate-and-frame filter press is communicated to the dryer through a pipeline, and the material outlet of the dryer is communicated to the iron phosphate storage tank through a pipeline.
9. An apparatus for producing inositol and iron phosphate according to claim 8, wherein: and a filtrate outlet of the third plate-and-frame filter press is communicated with a material inlet of the crystallization kettle through a pipeline.
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| CN202320457438.7U CN219784729U (en) | 2023-03-09 | 2023-03-09 | Iron phytate recovery unit and device of production inositol and ferric phosphate that uses it |
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| CN202320457438.7U CN219784729U (en) | 2023-03-09 | 2023-03-09 | Iron phytate recovery unit and device of production inositol and ferric phosphate that uses it |
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