CN118221084B - Method for producing monopotassium phosphate by using corn soaking water - Google Patents
Method for producing monopotassium phosphate by using corn soaking water Download PDFInfo
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- CN118221084B CN118221084B CN202410641665.4A CN202410641665A CN118221084B CN 118221084 B CN118221084 B CN 118221084B CN 202410641665 A CN202410641665 A CN 202410641665A CN 118221084 B CN118221084 B CN 118221084B
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- dihydrogen phosphate
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- potassium dihydrogen
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- 229910000402 monopotassium phosphate Inorganic materials 0.000 title claims abstract description 80
- 235000019796 monopotassium phosphate Nutrition 0.000 title claims abstract description 80
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 76
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 title claims abstract description 29
- 235000002017 Zea mays subsp mays Nutrition 0.000 title claims abstract description 29
- 235000005822 corn Nutrition 0.000 title claims abstract description 29
- GNSKLFRGEWLPPA-UHFFFAOYSA-M potassium dihydrogen phosphate Chemical compound [K+].OP(O)([O-])=O GNSKLFRGEWLPPA-UHFFFAOYSA-M 0.000 title claims abstract description 26
- LWIHDJKSTIGBAC-UHFFFAOYSA-K potassium phosphate Substances [K+].[K+].[K+].[O-]P([O-])([O-])=O LWIHDJKSTIGBAC-UHFFFAOYSA-K 0.000 title claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 238000002791 soaking Methods 0.000 title claims abstract description 12
- 240000008042 Zea mays Species 0.000 title claims description 27
- 239000012528 membrane Substances 0.000 claims abstract description 105
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 43
- 238000001728 nano-filtration Methods 0.000 claims abstract description 37
- 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 claims abstract description 32
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 32
- 235000002949 phytic acid Nutrition 0.000 claims abstract description 32
- 238000005406 washing Methods 0.000 claims abstract description 30
- CDAISMWEOUEBRE-UHFFFAOYSA-N scyllo-inosotol Natural products OC1C(O)C(O)C(O)C(O)C1O CDAISMWEOUEBRE-UHFFFAOYSA-N 0.000 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 claims abstract description 21
- 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 claims abstract description 21
- 229960000367 inositol Drugs 0.000 claims abstract description 21
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000011591 potassium Substances 0.000 claims abstract description 18
- 229910052700 potassium Inorganic materials 0.000 claims abstract description 18
- 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 15
- 239000000467 phytic acid Substances 0.000 claims abstract description 15
- 229940068041 phytic acid Drugs 0.000 claims abstract description 15
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims abstract description 13
- 238000001179 sorption measurement Methods 0.000 claims abstract description 12
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 11
- 230000007062 hydrolysis Effects 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims description 61
- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 claims description 54
- 239000000706 filtrate Substances 0.000 claims description 50
- 239000000047 product Substances 0.000 claims description 41
- 238000002425 crystallisation Methods 0.000 claims description 36
- 230000008025 crystallization Effects 0.000 claims description 36
- 238000001914 filtration Methods 0.000 claims description 36
- 239000008213 purified water Substances 0.000 claims description 27
- 239000012466 permeate Substances 0.000 claims description 26
- 238000003756 stirring Methods 0.000 claims description 26
- 238000001223 reverse osmosis Methods 0.000 claims description 24
- 239000013078 crystal Substances 0.000 claims description 22
- 239000012452 mother liquor Substances 0.000 claims description 21
- 238000001816 cooling Methods 0.000 claims description 19
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 18
- 239000011347 resin Substances 0.000 claims description 17
- 229920005989 resin Polymers 0.000 claims description 17
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 16
- 238000011010 flushing procedure Methods 0.000 claims description 16
- 239000007787 solid Substances 0.000 claims description 16
- 239000012530 fluid Substances 0.000 claims description 14
- 230000005484 gravity Effects 0.000 claims description 14
- 239000002699 waste material Substances 0.000 claims description 14
- 229920002472 Starch Polymers 0.000 claims description 12
- 230000001276 controlling effect Effects 0.000 claims description 12
- 235000019698 starch Nutrition 0.000 claims description 12
- 239000008107 starch Substances 0.000 claims description 12
- 241000196324 Embryophyta Species 0.000 claims description 10
- ONQDVAFWWYYXHM-UHFFFAOYSA-M potassium lauryl sulfate Chemical compound [K+].CCCCCCCCCCCCOS([O-])(=O)=O ONQDVAFWWYYXHM-UHFFFAOYSA-M 0.000 claims description 10
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 239000001103 potassium chloride Substances 0.000 claims description 8
- 235000011164 potassium chloride Nutrition 0.000 claims description 8
- 239000002253 acid Substances 0.000 claims description 7
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 6
- 230000003301 hydrolyzing effect Effects 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 claims description 4
- 125000003438 dodecyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 claims description 4
- 239000006228 supernatant Substances 0.000 claims description 2
- 239000000243 solution Substances 0.000 abstract description 43
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 12
- 239000011575 calcium Substances 0.000 abstract description 12
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract description 8
- 229910052791 calcium Inorganic materials 0.000 abstract description 8
- 239000011777 magnesium Substances 0.000 abstract description 8
- 229910052749 magnesium Inorganic materials 0.000 abstract description 8
- 238000000746 purification Methods 0.000 abstract description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 3
- 239000011574 phosphorus Substances 0.000 abstract description 3
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 3
- 102000004169 proteins and genes Human genes 0.000 abstract description 3
- 108090000623 proteins and genes Proteins 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- 239000003337 fertilizer Substances 0.000 abstract description 2
- 238000000034 method Methods 0.000 abstract description 2
- 241000209149 Zea Species 0.000 abstract 2
- 238000005352 clarification Methods 0.000 abstract 1
- 239000002920 hazardous waste Substances 0.000 abstract 1
- 239000011259 mixed solution Substances 0.000 abstract 1
- 238000007670 refining Methods 0.000 abstract 1
- 239000012465 retentate Substances 0.000 description 8
- 239000010413 mother solution Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000011049 filling Methods 0.000 description 4
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 3
- 229910001424 calcium ion Inorganic materials 0.000 description 3
- ZPWVASYFFYYZEW-UHFFFAOYSA-L dipotassium hydrogen phosphate Chemical compound [K+].[K+].OP([O-])([O-])=O ZPWVASYFFYYZEW-UHFFFAOYSA-L 0.000 description 3
- ZWPAJTZEGKKYAY-UHFFFAOYSA-N dodecapotassium;(2,3,4,5,6-pentaphosphonooxycyclohexyl) dihydrogen phosphate Chemical compound [K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].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 ZWPAJTZEGKKYAY-UHFFFAOYSA-N 0.000 description 3
- 229910001425 magnesium ion Inorganic materials 0.000 description 3
- 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 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- ODEGFPCTGGIJCF-UHFFFAOYSA-A P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+] Chemical compound P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].P(=O)([O-])([O-])[O-].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+].[K+] ODEGFPCTGGIJCF-UHFFFAOYSA-A 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000003456 ion exchange resin Substances 0.000 description 2
- 229920003303 ion-exchange polymer Polymers 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910000389 calcium phosphate Inorganic materials 0.000 description 1
- 239000013522 chelant Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000004042 decolorization Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- MHJAJDCZWVHCPF-UHFFFAOYSA-L dimagnesium phosphate Chemical compound [Mg+2].OP([O-])([O-])=O MHJAJDCZWVHCPF-UHFFFAOYSA-L 0.000 description 1
- 229910000395 dimagnesium phosphate Inorganic materials 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000001747 exhibiting effect Effects 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/30—Alkali metal phosphates
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/09—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis
- C07C29/12—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of esters of mineral acids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
- C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
- C07F9/02—Phosphorus compounds
- C07F9/06—Phosphorus compounds without P—C bonds
- C07F9/08—Esters of oxyacids of phosphorus
- C07F9/09—Esters of phosphoric acids
- C07F9/117—Esters of phosphoric acids with cycloaliphatic alcohols
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Inorganic Chemistry (AREA)
Abstract
The invention discloses a method for producing monopotassium phosphate by using corn soaking water, which relates to the technical field of monopotassium phosphate production, wherein the corn soaking water is subjected to anion exchange resin column adsorption phytic acid, purification water is used for washing columns to remove protein and most of calcium and magnesium, then 5% -30% wt potassium hydroxide solution is used for resolving, the pH value of the resolved solution is adjusted to be between 4.0 and 6.0, ultrafiltration membrane clarification treatment and nanofiltration membrane concentration are carried out, then hydrolysis is carried out at 150-180 ℃ to obtain high-quality inositol and monopotassium phosphate mixed solution, and separation and refining treatment are continued to obtain inositol products and monopotassium phosphate products. The monopotassium phosphate is simple to purify, the proportion of the phosphorus and the potassium is more balanced, the monopotassium phosphate is convenient to be used as fertilizer subsequently, the hazardous waste is produced in a small amount, and the method is environment-friendly.
Description
Technical Field
The invention relates to the technical field of potassium dihydrogen phosphate production, in particular to a method for producing potassium dihydrogen phosphate by using corn soaking water.
Background
It is common for a certain amount of phytic acid to be contained in the seeds, stems and stalks of plants. And can chelate divalent metal ions such as calcium, magnesium and the like to generate insoluble compounds, and can also form water-soluble compounds with monovalent metal ions such as potassium and the like in plants and form some complexes with proteins.
Phytic acid is phytate, and if pure products of inositol and monopotassium phosphate are to be produced, the pure product of phytic acid hexapotassium is required to be obtained, and the reaction equation is as follows:
it can be seen that there is also one hydrogen ion per phosphoric acid in the hexapotassium phytate molecule, so that the pH of hexapotassium phytate is between 4.0 and 4.6, exhibiting slight acidity. When the hexapotassium phytate is adsorbed on the alkaline ion exchange resin column, the hexapotassium phytate cannot be directly washed and desorbed unless chloride ions occupy the base of the resin, or the potassium hydroxide is excessive to generate the dodecapotassium phytate which is alkaline, so that the dodecapotassium phytate can be successfully resolved from the alkaline ion exchange resin column. However, the product of direct hydrolysis reaction of dodecapotassium phytate is inositol and dipotassium hydrogen phosphate, and the reaction equation is:
The product dipotassium hydrogen phosphate obtained here is difficult to crystallize due to the extremely high solubility. Simultaneously, dipotassium hydrogen phosphate belongs to a phosphate product with high potassium content, so that the proportion of phosphorus and potassium in the product is unbalanced.
The common production process at present uses potassium chloride and hydrochloric acid as resolving agents, and excessive chloride ions remain in the potassium phytate solution, so that excessive troubles and increase of treatment cost and reduction of product yield are brought to purification of hydrolyzed inositol and monopotassium phosphate products. In addition, because of small amount of chelated calcium and magnesium in the phytic acid, corresponding amount of calcium and magnesium hydrogen phosphate and phosphoric acid are generated after hydrolysis. In this case, the solubility of calcium and magnesium ions in the solution is large, which often causes the occurrence of turbid batch of the solubility of the potassium dihydrogen phosphate product, and affects the product quality.
Disclosure of Invention
The technical problems to be solved by the invention are as follows: aiming at the defects existing in the prior art, the method for producing the monopotassium phosphate by using the corn soaking water is provided, and the obtained monopotassium phosphate product has good quality and high yield.
In order to solve the technical problems, the technical scheme of the invention is as follows:
A method for producing monopotassium phosphate by using corn steep water, comprising the following steps:
a: allowing supernatant of the settled corn soaking water to enter an anion exchange resin column for phytic acid adsorption, and collecting effluent;
b: countercurrent flushing of the adsorbed anion exchange resin column with purified water;
C: analyzing the anion exchange resin column by using potassium hydroxide solution with the concentration of 5-30%wt, and collecting the potassium dodecyl phytate analysis solution;
d: dropwise adding an acid solution into the potassium dodecyl sulfate analytical solution, controlling the dropwise adding time to be 30-60 min, and regulating the pH value of the system to be between 4.0 and 6.0 to obtain an acidizing fluid;
e: clarifying the acidified liquid by an ultrafiltration membrane to obtain ultrafiltration membrane trapped liquid and ultrafiltration membrane permeate liquid, concentrating the ultrafiltration membrane permeate liquid by a nanofiltration membrane, and collecting the nanofiltration membrane permeate liquid and the nanofiltration membrane trapped liquid;
F: hydrolyzing the nanofiltration membrane trapped fluid at 150-180deg.C for 5-15h, filtering to remove waste residue, and collecting hydrolysis filtrate;
G: separating the hydrolyzed filtrate by a chromatographic resin simulated moving bed to obtain an inositol phase and a potassium dihydrogen phosphate phase, concentrating the potassium dihydrogen phosphate phase to a specific gravity of 30-40 Baume under the conditions of a temperature of 50-100 ℃ and a vacuum of-0.06-0.09 MPa, stirring and cooling to 25-30 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain a potassium dihydrogen phosphate product I.
Preferably, the feeding flow rate of the corn steep water in the step A is 1-2BV/h, and the anion exchange resin column is a gel type weak alkaline acrylic anion exchange resin column.
Preferably, the purified water is fed in step B at a flow rate of 1-15 BV/h and in an amount of 1.5-5BV.
Preferably, in the step B, the anion exchange resin column after adsorption is subjected to countercurrent flushing by purified water, washing water is collected, washing filtrate is collected after washing water is filtered, and the washing filtrate enters a reverse osmosis membrane until the solid content of the interception liquid of the reverse osmosis membrane is the same as that of the effluent liquid in the step A;
the reverse osmosis membrane permeate is used for next batch of purified water for washing the anion exchange resin column;
and (3) returning the reverse osmosis membrane trapped liquid and the effluent liquid in the step A and the ultrafiltration membrane trapped liquid in the step E to a starch plant.
Preferably, the feeding speed of the potassium hydroxide solution in the step C is 0.5-1 BV/h, and the average pH value of the potassium dodecyl sulfate solution is controlled to be 8-12.
The acid solution in the step D is phosphoric acid solution;
Concentrating the nanofiltration membrane permeation solution in the step E to a specific gravity of 30-40 Baume at a temperature of 50-100 ℃ and a vacuum of-0.06-0.09 MPa, then stirring and cooling to 25-30 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain a potassium dihydrogen phosphate product II;
The specific reaction equation is:
And (3) continuously distilling, concentrating and crystallizing the centrifugal mother liquor obtained after centrifugal filtration of the crystallization feed liquid until the filtrate is concentrated until no granular crystals are formed, and collecting the obtained crystals to a potassium dihydrogen phosphate product II.
Preferably, the acid solution in the step D is hydrochloric acid solution;
Concentrating the nanofiltration membrane permeate in the step E into a potassium chloride solution at the temperature of 50-100 ℃ and the vacuum of-0.06-0.09 MPa until the specific gravity is 30-40 Baume, then stirring and cooling to 25-30 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain a potassium chloride product;
The specific reaction equation is:
And (3) continuously distilling, concentrating and crystallizing the centrifugal mother liquor obtained after centrifugal filtration of the crystallization feed liquid until the filtrate is concentrated until no granular crystals are formed, and collecting the obtained crystals to a potassium chloride product.
Preferably, the molecular weight cut-off of the ultrafiltration membrane in the step E is 100000-200000, and the molecular weight cut-off of the nanofiltration membrane is 300-1500;
and E, thoroughly washing the ultrafiltration membrane trapped liquid by using purified water, combining the permeate water with the ultrafiltration membrane permeate liquid, and then entering a nanofiltration membrane, wherein the thoroughly washed ultrafiltration membrane trapped liquid returns to a ring starch plant.
Preferably, the centrifugal mother liquor obtained after the centrifugal filtration of the crystallization feed liquid in the step G is distilled, concentrated and crystallized continuously until the filtrate is concentrated until no granular crystals are formed, and the obtained crystals are collected to a potassium dihydrogen phosphate product I.
Preferably, the inositol phase in the step G is concentrated to the density of 18-30 Baume under the vacuum of-0.06-0.09 MPa at the temperature of 50-100 ℃, medicinal active carbon with the solid content of 2% w/w is added by stirring, decolorization is carried out for 0.5-1 h at the temperature of 80-95 ℃, the active carbon is removed by filtering while the solution is hot, the filtrate is cooled to the temperature of 25-30 ℃ by stirring, and centrifugally filtered, thus obtaining an inositol product;
And (5) returning the centrifugal mother liquor to the chromatographic resin simulated moving bed.
Due to the adoption of the technical scheme, the invention has the beneficial effects that:
1. The potassium hydroxide solution is adopted to analyze the anion exchange resin column to obtain the potassium phytate analysis solution, then the acid solution is dripped to convert the potassium phytate into the potassium hexaphytate to obtain the potassium salt, then the potassium phytate and the potassium salt are subjected to membrane separation, and finally the potassium phytate is hydrolyzed to obtain the inositol and the potassium dihydrogen phosphate, so that the potassium dihydrogen phosphate has small solubility and simple crystallization treatment. Meanwhile, the proportion of phosphorus and potassium in the monopotassium phosphate is more balanced, so that the monopotassium phosphate is convenient to be used as a fertilizer in the follow-up process.
2. The potassium phytate analysis solution is acidified by phosphoric acid to obtain chlorine-free ions and salts thereof in the potassium phytate, the separation and purification are simple, the purity of the product is increased, in addition, a small amount of calcium and magnesium ions in the potassium phytate after hydrolysis can form calcium hydrophosphate and magnesium hydrophosphate, and the calcium and magnesium ions are directly filtered and removed, so that the quality of the potassium dihydrogen phosphate product is further improved.
3. The potassium dihydrogen phosphate analytical solution is acidified by phosphoric acid to obtain potassium hexaphosphate and potassium dihydrogen phosphate, the amount of the potassium dihydrogen phosphate obtained by acidification is 95% of the yield of the potassium dihydrogen phosphate obtained by subsequent hydrolysis of the potassium hexaphosphate, the product of the potassium dihydrogen phosphate is greatly increased, the economic value of the potassium dihydrogen phosphate is higher, and the economic benefit is improved.
4. The centrifugal mother liquor after the purification of the monopotassium phosphate is subjected to distillation, concentration and crystallization again, the monopotassium phosphate is extracted again, the waste of raw materials is greatly reduced, the yield of the monopotassium phosphate is improved, the production quantity of dangerous waste is reduced, and the final weight of the dangerous waste is within 10% of the total yield of the monopotassium phosphate.
Drawings
FIG. 1 is a liquid chromatogram of the inositol product of example 3 of the present invention.
Detailed Description
The invention is further illustrated by the following examples.
Example 1
A method for producing monopotassium phosphate by using corn steep water, comprising the following steps:
A:650L corn soaking water (phytic acid content 1%w/v) enters a gel type weak alkaline acrylic anion exchange resin column ZG312 of a resin filling 45L at a flow rate of 1BV/h to carry out phytic acid adsorption, 650L effluent is collected, and the solid content is 13%w/w;
B: countercurrent flushing is carried out on the anion exchange resin column after adsorption by using 1.5BV of purified water, the feeding flow rate of the purified water is 1BV/h, 67.5L of washing water is collected, 67L of flushing filtrate is collected after washing water is filtered, and the flushing filtrate enters a reverse osmosis membrane until the solid content of the intercepting liquid of the reverse osmosis membrane is the same as that of the effluent liquid in the step A; returning the reverse osmosis membrane retentate 36L to the starch mill with the effluent from step a;
The reverse osmosis membrane permeate 31L was used for the next batch of purified water for washing the anion exchange resin column.
C: analyzing the anion exchange resin column by using a potassium hydroxide solution with the concentration of 5%wt at the flow rate of 0.5BV/h, controlling the average pH value of the analysis solution to be 8, and collecting 91.8L of the potassium dodecyl sulfate analysis solution;
D: adding 85% industrial phosphoric acid into the potassium dodecyl sulfate solution dropwise, controlling the dropwise adding time to be 30min, and regulating the pH value of the system to be between 6.0 to obtain 94.6L of acidizing fluid;
E: clarifying the acidified solution by an ultrafiltration membrane with the molecular weight cutoff of 100000 to obtain 2.8L of ultrafiltration membrane cutoff and 91.8L of ultrafiltration membrane permeation solution, washing the ultrafiltration membrane cutoff by purified water, merging the washing water and the ultrafiltration membrane permeation solution, concentrating by 101.8L of nanofiltration membrane with the molecular weight cutoff of 300, collecting 79.3L of nanofiltration membrane permeation solution and 22.5L of nanofiltration membrane cutoff, and returning 2.8L of the washed ultrafiltration membrane cutoff to a ring starch plant;
f: hydrolyzing the nanofiltration membrane trapped fluid for 5 hours at 150 ℃, filtering to remove waste residues, and collecting 22.3L of hydrolysis filtrate, wherein the inositol content in the hydrolysis filtrate is 50g/L, 236g/L of monopotassium phosphate contains 0.8% of protein, 19ppm of calcium and 168ppm of magnesium;
G: separating the hydrolyzed filtrate by a chromatographic resin simulated moving bed to obtain an inositol phase 17L and a potassium dihydrogen phosphate phase 68.8L, wherein the potassium dihydrogen phosphate phase is concentrated to have a specific gravity of 30 Baume at a temperature of 50 ℃ and a vacuum of-0.06-0.09 MPa, then stirring and cooling to 25 ℃ for crystallization, and the obtained crystallization liquid is centrifugally filtered to obtain a potassium dihydrogen phosphate product I3.95 kg, a purity of 98.5%, a yield of 70% and a centrifugal mother liquid I5.9L.
Concentrating nanofiltration membrane permeate liquid to a specific gravity of 30 Baume under the conditions of a temperature of 50 ℃ and a vacuum of-0.06-0.09 MPa, stirring and cooling to 25 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain 3.78kg of potassium dihydrogen phosphate product II, a purity of 99.5%, a yield of 68% and 5.2L of centrifugal mother liquor II.
And (3) continuously distilling, concentrating and crystallizing after the first centrifugal mother liquor and the second centrifugal mother liquor are collected until the filtrate is concentrated until no granular crystals are formed, thus obtaining 1.81kg of potassium dihydrogen phosphate crystals and finally 2.12kg of filtrate for waste treatment.
Concentrating inositol phase to density 18 Baume under vacuum-0.06-0.09 MPa at 50deg.C, adding medicinal active carbon with solid content of 2% w/w under stirring, decolorizing at 80deg.C for 0.5 hr, filtering while hot, cooling the filtrate under stirring, crystallizing to 25deg.C, centrifuging, and filtering to obtain inositol product 1.166kg with purity 99.6%, yield 95%, and centrifuging mother liquor three 1.2L;
three times of sleeving the centrifugal mother solution the chromatographic resin simulates a moving bed.
Example 2
A method for producing monopotassium phosphate by using corn steep water, comprising the following steps:
a:650L corn soaking water (phytic acid content 1% w/v) enters a gel type weak alkaline acrylic anion exchange resin column ZG312 of a resin filling 45L at a flow rate of 1.5BV/h to carry out phytic acid adsorption, and 650L effluent is collected, wherein the solid content is 13% w/w;
B: carrying out countercurrent flushing on the anion exchange resin column after adsorption by using 3BV of purified water, wherein the feeding flow rate of the purified water is 5BV/h, collecting washing water 135L, filtering the washing water, collecting flushing filtrate 134L, and enabling the flushing filtrate to enter a reverse osmosis membrane until the solid content of the reverse osmosis membrane trapped fluid is the same as that of the effluent in the step A; returning the reverse osmosis membrane retentate 36L to the starch mill with the effluent from step a;
Reverse osmosis membrane permeate 98L was used for the next batch of purified water for washing the anion exchange resin column.
C: analyzing the anion exchange resin column by using a potassium hydroxide solution with the concentration of 20%wt at the flow rate of 0.8BV/h, controlling the average pH value of the analysis solution to be 10, and collecting 23L of potassium dodecyl sulfate analysis solution;
D: adding 85% industrial phosphoric acid into the potassium dodecyl sulfate solution dropwise, controlling the dropwise adding time to be 50min, and regulating the pH value of the system to be between 5.0 to obtain 25.8L of acidizing fluid;
E: clarifying the acidified solution by an ultrafiltration membrane with a molecular weight cutoff of 150000 to obtain 2.8L of ultrafiltration membrane cutoff and 23L of ultrafiltration membrane permeation solution, washing the ultrafiltration membrane cutoff by purified water, merging the permeation water with the ultrafiltration membrane permeation solution, concentrating by 33L of nanofiltration membrane with a molecular weight cutoff of 1000, collecting 10.5L of nanofiltration membrane permeation solution and 22.5L of nanofiltration membrane cutoff, and returning 2.8L of the washed ultrafiltration membrane cutoff to a ring starch plant;
f: hydrolyzing the nanofiltration membrane trapped fluid for 10 hours at 170 ℃, filtering to remove waste residues, and collecting 22.3L of hydrolysis filtrate, wherein the inositol content in the hydrolysis filtrate is 53.6g/L, the monopotassium phosphate is 246g/L, the protein content is 0.5%, the calcium content is 15ppm, and the magnesium content is 108ppm;
G: separating the hydrolyzed filtrate by a chromatographic resin simulated moving bed to obtain an inositol phase 17L and a potassium dihydrogen phosphate phase 69L, wherein the potassium dihydrogen phosphate phase is concentrated to have a specific gravity of 35 Baume at a temperature of 80 ℃ and a vacuum of-0.06-0.09 MPa, then stirring and cooling to 28 ℃ for crystallization, and the obtained crystallization liquid is centrifugally filtered to obtain 4.16g of potassium dihydrogen phosphate product I, 99.1% of purity, 75% of yield and 6.3L of centrifugal mother liquid I.
Concentrating nanofiltration membrane permeate liquid to a specific gravity of 35 Baume under the conditions of a temperature of 80 ℃ and a vacuum of-0.06-0.09 MPa, stirring and cooling to 28 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain 4.06kg of potassium dihydrogen phosphate product II, a purity of 99.2%, a yield of 73% and 7.2L of centrifugal mother liquid II.
And (3) continuously distilling, concentrating and crystallizing after the first centrifugal mother liquor and the second centrifugal mother liquor are collected until the filtrate is concentrated until no granular crystals are formed, so that 3.18kg of potassium dihydrogen phosphate crystals are obtained, and finally, 2.12kg of filtrate is subjected to waste treatment.
Concentrating inositol phase to density of 25 Baume under vacuum of-0.06-0.09 MPa at 80deg.C, adding medicinal active carbon with solid content of 2% w/w under stirring, decolorizing at 90deg.C for 0.8 hr, filtering while hot, cooling filtrate under stirring, crystallizing to 28deg.C, centrifuging, and filtering to obtain inositol product 1.202kg with purity of 99.7%, yield of 98%, and centrifuging mother liquor three 1.1L;
three times of sleeving the centrifugal mother solution the chromatographic resin simulates a moving bed.
Example 3
A method for producing monopotassium phosphate by using corn steep water, comprising the following steps:
A:650L corn soaking water (phytic acid content 1%w/v) enters a gel type weak alkaline acrylic anion exchange resin column ZG312 of a resin filling 45L at a flow rate of 2BV/h to carry out phytic acid adsorption, 650L effluent is collected, and the solid content is 13%w/w;
B: carrying out countercurrent flushing on the anion exchange resin column after adsorption by using 5BV of purified water, wherein the feeding flow rate of the purified water is 15BV/h, collecting washing water 225L, filtering the washing water, collecting flushing filtrate 223L, and leading the flushing filtrate to enter a reverse osmosis membrane until the solid content of the reverse osmosis membrane trapped liquid is the same as that of the effluent liquid in the step A; returning the reverse osmosis membrane retentate 36L to the starch mill with the effluent from step a;
reverse osmosis membrane permeate 187L was used for the next batch of purified water for washing the anion exchange resin column.
C: analyzing the anion exchange resin column with 30% wt potassium hydroxide solution at a flow rate of 1 BV/h, controlling the average pH value of the analysis solution to be 12, and collecting 28.3L of potassium dodecyl phytate analysis solution;
D: adding 85% industrial phosphoric acid into the potassium dodecyl sulfate solution dropwise, controlling the dropwise adding time to be 60min, and regulating the pH value of the system to be between 4.0 to obtain 31.1L of acidizing fluid;
E: clarifying the acidified solution by an ultrafiltration membrane with a molecular weight cutoff of 200000 to obtain 2.2L of ultrafiltration membrane retentate and 28.9L of ultrafiltration membrane permeate, washing the ultrafiltration membrane retentate with purified water, merging the permeate water with the ultrafiltration membrane permeate, concentrating 38.9L of the permeate water by a nanofiltration membrane with a molecular weight cutoff of 1500, and collecting 16.4L of nanofiltration membrane permeate and 22.5L of nanofiltration membrane retentate, wherein 2.2L of the washed ultrafiltration membrane retentate is returned to a ring starch plant;
F: hydrolyzing the nanofiltration membrane trapped fluid for 15 hours at 180 ℃, filtering to remove waste residues, and collecting 22.3L of hydrolyzed filtrate, wherein the inositol content in the hydrolyzed filtrate is 54.6g/L, the potassium dihydrogen phosphate content is 247.6g/L, the protein content is 0.1%, the calcium content is 11ppm, and the magnesium content is 68ppm;
g: separating the hydrolyzed filtrate by a chromatographic resin simulated moving bed to obtain an inositol phase 17L and a potassium dihydrogen phosphate phase 70L, wherein the potassium dihydrogen phosphate phase is concentrated to have a specific gravity of 40 Baume at a temperature of 100 ℃ and a vacuum of-0.06-0.09 MPa, then stirring and cooling to 30 ℃ for crystallization, and the obtained crystallization liquid is centrifugally filtered to obtain 4.06kg of potassium dihydrogen phosphate product I, the purity is 99.5%, the yield is 73%, and the centrifugal mother liquid I is 5.9L.
Concentrating nanofiltration membrane permeate to a specific gravity of 40 Baume at a temperature of 100 ℃ and a vacuum of 0.09MPa, stirring and cooling to 30 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain 4.37kg of potassium dihydrogen phosphate product II, wherein the purity is 99.5%, the yield is 68%, and the centrifugal mother liquid II is 5.2L.
And (3) continuously distilling, concentrating and crystallizing after the first centrifugal mother liquor and the second centrifugal mother liquor are collected until the filtrate is concentrated until no granular crystals are formed, so that 3.65kg of potassium dihydrogen phosphate crystals are obtained, and finally, 2.12kg of filtrate is subjected to waste treatment.
Concentrating inositol phase to density of 30 Baume under vacuum of-0.06-0.09 MPa at 100deg.C, adding medicinal active carbon with solid content of 2% w/w under stirring, decolorizing at 95deg.C for 1 hr, filtering while hot, cooling and crystallizing filtrate under stirring to 30deg.C, centrifuging, filtering to obtain inositol product 1.18kg with purity of 99.8%, yield of 96.8%, centrifuging mother liquor of three 1.16L;
three times of sleeving the centrifugal mother solution the chromatographic resin simulates a moving bed.
Example 4
A method for producing monopotassium phosphate by using corn steep water, comprising the following steps:
A:650L corn soaking water (phytic acid content 1%w/v) enters a gel type weak alkaline acrylic anion exchange resin column ZG312 of a resin filling 45L at a flow rate of 2BV/h to carry out phytic acid adsorption, 650L effluent is collected, and the solid content is 13%w/w;
B: carrying out countercurrent flushing on the anion exchange resin column after adsorption by using 5BV of purified water, wherein the feeding flow rate of the purified water is 15 BV/h, collecting washing water 225L, filtering the washing water, collecting flushing filtrate 223L, and leading the flushing filtrate to enter a reverse osmosis membrane until the solid content of the reverse osmosis membrane trapped fluid is the same as that of the effluent in the step A; returning the reverse osmosis membrane retentate 36L to the starch mill with the effluent from step a;
reverse osmosis membrane permeate 187L was used for the next batch of purified water for washing the anion exchange resin column.
C: analyzing the anion exchange resin column with 25% wt potassium hydroxide solution at a flow rate of 1 BV/h, controlling the average pH value of the analysis solution to be 10, and collecting 28.36L of potassium dodecyl phytate analysis solution;
D: dropwise adding 30% industrial hydrochloric acid into the potassium dodecyl sulfate analytic solution, controlling the dropwise adding time to be 60min, and regulating the pH value of the system to be between 4.0 to obtain 31.2L of acidizing fluid;
E: clarifying the acidified solution by an ultrafiltration membrane with a molecular weight cutoff of 150000 to obtain 2.3L of ultrafiltration membrane cutoff and 28.9L of ultrafiltration membrane permeation solution, washing the ultrafiltration membrane cutoff by purified water, merging the permeation water and the ultrafiltration membrane permeation solution, concentrating by 38L of nanofiltration membrane with a molecular weight cutoff of 1000, collecting 15.5L of nanofiltration membrane permeation solution and 22.5L of nanofiltration membrane cutoff, and returning 2.3L of the washed ultrafiltration membrane cutoff to a ring starch plant;
F: hydrolyzing the nanofiltration membrane trapped fluid for 12 hours at 170 ℃, filtering to remove waste residues, and collecting 22.3L of hydrolyzed filtrate, wherein the inositol content in the hydrolyzed filtrate is 54.3g/L, the potassium dihydrogen phosphate is 243.6g/L, the protein content is 0.1%, the calcium content is 12ppm, and the magnesium content is 71ppm;
G: separating the hydrolyzed filtrate by a chromatographic resin simulated moving bed to obtain an inositol phase 17L and a potassium dihydrogen phosphate phase 69L, wherein the potassium dihydrogen phosphate phase is concentrated to have a specific gravity of 35 Baume at a temperature of 90 ℃ and a vacuum of-0.06-0.09 MPa, then stirring and cooling to 28 ℃ for crystallization, and the obtained crystallization liquid is centrifugally filtered to obtain 4.06kg of potassium dihydrogen phosphate product I, the purity is 99.7%, the yield is 73%, and the centrifugal mother liquid I is 6.1L.
Concentrating the nanofiltration membrane permeate to a specific gravity of 32 Baume at a temperature of 100 ℃ and a vacuum of-0.06-0.09 MPa, stirring and cooling to 25 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain 1.91g of potassium chloride product with a purity of 99.2%, a yield of 68% and 5.6L of centrifugal mother liquor.
And (3) continuously distilling, concentrating and crystallizing the centrifugal mother solution until the filtrate is concentrated until no granular crystals are formed, thus obtaining 1.51kg of potassium dihydrogen phosphate crystals and finally 1.2kg of filtrate for waste treatment.
And (3) continuing to distill, concentrate and crystallize the second centrifugal mother solution until the filtrate is concentrated until no more granular crystals are formed, thus obtaining 0.846kg of potassium chloride crystals and finally 1.1kg of filtrate for waste treatment.
Concentrating inositol phase to density of 25 Baume under vacuum of-0.06-0.09 MPa at 90 deg.C, adding medicinal active carbon with solid content of 2% w/w under stirring, decolorizing at 90 deg.C for 1 hr, filtering while hot, cooling filtrate under stirring, crystallizing to 25 deg.C, centrifuging, filtering to obtain inositol product 1.203kg with purity of 99.7%, yield of 98%, centrifuging mother liquor of three 1.3L;
three times of sleeving the centrifugal mother solution the chromatographic resin simulates a moving bed.
It is to be understood that these examples are illustrative of the present application and are not intended to limit the scope of the present application. 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 application, and such equivalents are intended to fall within the scope of the application as defined in the appended claims.
Claims (10)
1. A method for producing monopotassium phosphate by using corn steep water, which is characterized by comprising the following steps:
a: allowing supernatant of the settled corn soaking water to enter an anion exchange resin column for phytic acid adsorption, and collecting effluent;
b: countercurrent flushing of the adsorbed anion exchange resin column with purified water;
C: analyzing the anion exchange resin column by using potassium hydroxide solution with the concentration of 5-30%wt, and collecting the potassium dodecyl phytate analysis solution;
d: dropwise adding an acid solution into the potassium dodecyl sulfate analytical solution, controlling the dropwise adding time to be 30-60 min, and regulating the pH value of the system to be between 4.0 and 6.0 to obtain an acidizing fluid;
e: clarifying the acidified liquid by an ultrafiltration membrane to obtain ultrafiltration membrane trapped liquid and ultrafiltration membrane permeate liquid, concentrating the ultrafiltration membrane permeate liquid by a nanofiltration membrane, and collecting the nanofiltration membrane permeate liquid and the nanofiltration membrane trapped liquid;
F: hydrolyzing the nanofiltration membrane trapped fluid at 150-180deg.C for 5-15h, filtering to remove waste residue, and collecting hydrolysis filtrate;
G: separating the hydrolyzed filtrate by a chromatographic resin simulated moving bed to obtain an inositol phase and a potassium dihydrogen phosphate phase, concentrating the potassium dihydrogen phosphate phase to a specific gravity of 30-40 poise at a temperature of 50-100 ℃ and a vacuum of-0.06-0.09 MPa, stirring and cooling to 25-30 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain a potassium dihydrogen phosphate product I.
2. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: the feeding flow rate of the corn steep water in the step A is 1-2BV/h, and the anion exchange resin column is a gel type weak alkaline acrylic anion exchange resin column.
3. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: the feeding flow rate of the purified water in the step B is 1-15 BV/h, and the consumption of the purified water is 1.5-5BV.
4. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: in the step B, the absorbed anion exchange resin column is subjected to countercurrent flushing by purified water, washing water is collected, washing filtrate is collected after washing water is filtered, and the washing filtrate enters a reverse osmosis membrane until the solid content of the interception liquid of the reverse osmosis membrane is the same as that of the effluent liquid in the step A;
the reverse osmosis membrane permeate is used for next batch of purified water for washing the anion exchange resin column;
and (3) returning the reverse osmosis membrane trapped liquid and the effluent liquid in the step A and the ultrafiltration membrane trapped liquid in the step E to a starch plant.
5. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: and C, controlling the feeding speed of the potassium hydroxide solution to be 0.5-1 BV/h and controlling the average pH value of the potassium dodecyl sulfate solution to be 8-12.
6. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: the acid solution in the step D is phosphoric acid solution;
Concentrating the nanofiltration membrane permeation solution in the step E to a specific gravity of 30-40 poise at a temperature of 50-100 ℃ and a vacuum of-0.06-0.09 MPa, stirring and cooling to 25-30 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain a potassium dihydrogen phosphate product II;
And (3) continuously distilling, concentrating and crystallizing the centrifugal mother liquor obtained after centrifugal filtration of the crystallization feed liquid until the filtrate is concentrated until no granular crystals are formed, and collecting the obtained crystals to a potassium dihydrogen phosphate product II.
7. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: the acid solution in the step D is hydrochloric acid solution;
concentrating the nanofiltration membrane permeation solution in the step E to a specific gravity of 30-40 poise at a temperature of 50-100 ℃ and a vacuum of-0.06-0.09 MPa, stirring and cooling to 25-30 ℃ for crystallization, and centrifugally filtering the obtained crystallization feed liquid to obtain a potassium chloride product;
And (3) continuously distilling, concentrating and crystallizing the centrifugal mother liquor obtained after centrifugal filtration of the crystallization feed liquid until the filtrate is concentrated until no granular crystals are formed, and collecting the obtained crystals to a potassium chloride product.
8. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: the molecular weight cut-off of the ultrafiltration membrane in the step E is 100000-200000, and the molecular weight cut-off of the nanofiltration membrane is 300-1500;
And E, thoroughly washing the ultrafiltration membrane trapped liquid in the step with purified water, combining the permeate water with the ultrafiltration membrane permeate liquid, and then entering a nanofiltration membrane, wherein the thoroughly washed ultrafiltration membrane trapped liquid is returned to a starch plant.
9. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: and G, continuously distilling, concentrating and crystallizing the centrifugal mother liquor obtained by centrifugally filtering the crystallization feed liquid in the step G until the filtrate is concentrated until no granular crystals are formed, and collecting the obtained crystals into a potassium dihydrogen phosphate product I.
10. A method for producing potassium dihydrogen phosphate using corn steep water as defined in claim 1, wherein: concentrating the inositol phase in the step G to the density of 18-30 poise under the vacuum of-0.06-0.09 MPa at the temperature of 50-100 ℃, adding medicinal active carbon with the solid content of 2% w/w under stirring, decoloring for 0.5-1 h at the temperature of 80-95 ℃, filtering while the active carbon is removed, cooling and crystallizing the filtrate under stirring to the temperature of 25-30 ℃, and centrifugally filtering to obtain an inositol product;
And (5) returning the centrifugal mother liquor to the chromatographic resin simulated moving bed.
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