CN114699801B - Valve array type continuous ion exchange system for purification of red lactic acid - Google Patents
Valve array type continuous ion exchange system for purification of red lactic acid Download PDFInfo
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- CN114699801B CN114699801B CN202210631978.2A CN202210631978A CN114699801B CN 114699801 B CN114699801 B CN 114699801B CN 202210631978 A CN202210631978 A CN 202210631978A CN 114699801 B CN114699801 B CN 114699801B
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- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 title claims abstract description 274
- 235000014655 lactic acid Nutrition 0.000 title claims abstract description 137
- 239000004310 lactic acid Substances 0.000 title claims abstract description 137
- 238000005342 ion exchange Methods 0.000 title claims abstract description 54
- 238000000746 purification Methods 0.000 title description 9
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 171
- 238000001179 sorption measurement Methods 0.000 claims abstract description 75
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 66
- 230000008929 regeneration Effects 0.000 claims abstract description 64
- 238000011069 regeneration method Methods 0.000 claims abstract description 64
- 238000003795 desorption Methods 0.000 claims abstract description 37
- 239000011347 resin Substances 0.000 claims abstract description 33
- 229920005989 resin Polymers 0.000 claims abstract description 33
- 238000004458 analytical method Methods 0.000 claims abstract description 32
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 26
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 26
- JVTAAEKCZFNVCJ-UHFFFAOYSA-M Lactate Chemical compound CC(O)C([O-])=O JVTAAEKCZFNVCJ-UHFFFAOYSA-M 0.000 claims abstract description 17
- 239000002699 waste material Substances 0.000 claims abstract description 13
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 9
- -1 lactate ions Chemical class 0.000 claims abstract description 7
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 138
- 239000000243 solution Substances 0.000 claims description 97
- 238000005406 washing Methods 0.000 claims description 79
- 239000000463 material Substances 0.000 claims description 45
- 238000011001 backwashing Methods 0.000 claims description 43
- 239000002253 acid Substances 0.000 claims description 39
- 238000002386 leaching Methods 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 11
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 11
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 11
- 238000000855 fermentation Methods 0.000 claims description 9
- 230000004151 fermentation Effects 0.000 claims description 9
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 239000000706 filtrate Substances 0.000 claims description 8
- 238000007670 refining Methods 0.000 claims description 7
- 239000011159 matrix material Substances 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 4
- 238000004042 decolorization Methods 0.000 claims description 3
- 238000010790 dilution Methods 0.000 claims description 3
- 239000012895 dilution Substances 0.000 claims 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 abstract description 8
- 239000003456 ion exchange resin Substances 0.000 abstract description 8
- 229920003303 ion-exchange polymer Polymers 0.000 abstract description 8
- 102000004169 proteins and genes Human genes 0.000 abstract description 5
- 108090000623 proteins and genes Proteins 0.000 abstract description 5
- 150000003839 salts Chemical class 0.000 abstract description 4
- 150000004676 glycans Chemical class 0.000 abstract description 2
- 229920001282 polysaccharide Polymers 0.000 abstract description 2
- 239000005017 polysaccharide Substances 0.000 abstract description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 13
- 239000008367 deionised water Substances 0.000 description 11
- 229910021641 deionized water Inorganic materials 0.000 description 11
- 239000002585 base Substances 0.000 description 8
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 6
- 229910021529 ammonia Inorganic materials 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 239000003480 eluent Substances 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- 239000012492 regenerant Substances 0.000 description 6
- 230000001172 regenerating effect Effects 0.000 description 6
- 239000012535 impurity Substances 0.000 description 5
- JVTAAEKCZFNVCJ-REOHCLBHSA-N L-lactic acid Chemical compound C[C@H](O)C(O)=O JVTAAEKCZFNVCJ-REOHCLBHSA-N 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000000199 molecular distillation Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000005374 membrane filtration Methods 0.000 description 3
- 239000000049 pigment Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 235000000346 sugar Nutrition 0.000 description 3
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000007865 diluting Methods 0.000 description 2
- 238000010828 elution Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 150000008163 sugars Chemical class 0.000 description 2
- KVZLHPXEUGJPAH-BXRBKJIMSA-N (2s)-2-oxidanylpropanoic acid Chemical compound C[C@H](O)C(O)=O.C[C@H](O)C(O)=O KVZLHPXEUGJPAH-BXRBKJIMSA-N 0.000 description 1
- 241001550224 Apha Species 0.000 description 1
- 229920002261 Corn starch Polymers 0.000 description 1
- 241000124008 Mammalia Species 0.000 description 1
- CZMRCDWAGMRECN-UHFFFAOYSA-N Rohrzucker Natural products OCC1OC(CO)(OC2OC(CO)C(O)C(O)C2O)C(O)C1O CZMRCDWAGMRECN-UHFFFAOYSA-N 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 229930006000 Sucrose Natural products 0.000 description 1
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- WDIHJSXYQDMJHN-UHFFFAOYSA-L barium chloride Chemical compound [Cl-].[Cl-].[Ba+2] WDIHJSXYQDMJHN-UHFFFAOYSA-L 0.000 description 1
- 229910001626 barium chloride Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000008120 corn starch Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- DQYBDCGIPTYXML-UHFFFAOYSA-N ethoxyethane;hydrate Chemical compound O.CCOCC DQYBDCGIPTYXML-UHFFFAOYSA-N 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 235000013336 milk Nutrition 0.000 description 1
- 239000008267 milk Substances 0.000 description 1
- 210000004080 milk Anatomy 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 235000013379 molasses Nutrition 0.000 description 1
- 231100000957 no side effect Toxicity 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 229960004793 sucrose Drugs 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/47—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
- B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
- B01D15/1864—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using two or more columns
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
- B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
- B01D15/1864—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using two or more columns
- B01D15/1871—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using two or more columns placed in series
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
- B01D15/36—Selective adsorption, e.g. chromatography characterised by the separation mechanism involving ionic interaction
- B01D15/361—Ion-exchange
- B01D15/363—Anion-exchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/42—Selective adsorption, e.g. chromatography characterised by the development mode, e.g. by displacement or by elution
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/42—Selective adsorption, e.g. chromatography characterised by the development mode, e.g. by displacement or by elution
- B01D15/424—Elution mode
- B01D15/426—Specific type of solvent
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J41/00—Anion exchange; Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
- B01J41/04—Processes using organic exchangers
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention discloses a valve array type continuous ion exchange system for purifying red lactic acid, which comprises an adsorption area, an analysis area and a regeneration area, wherein each area comprises at least one anion exchange resin column; the feed of the anion exchange resin column in the adsorption zone is a red lactic acid solution, the anion exchange resin column in the desorption zone adsorbs lactate, the feed is a sulfuric acid solution, the anion exchange resin column in the regeneration zone adsorbs sulfate, and the feed is an ammonia water solution; and the anion exchange resin column in the adsorption zone is switched to the desorption zone after adsorbing lactate and being saturated, the lactate ions on the anion exchange resin column in the desorption zone are switched to the regeneration zone after being desorbed, and the anion exchange resin column in the regeneration zone is switched to the adsorption zone after being regenerated. The system continuously operates by switching the resin subareas and the resin columns, utilizes the groups on the ion exchange resin to adsorb lactate, directly separates the lactic acid from protein, polysaccharide and salts in the red lactic acid solution, changes waste into valuable, and improves the yield of the lactic acid.
Description
Technical Field
The invention relates to a lactic acid separation and purification technology, in particular to a valve array type continuous ion exchange system for purifying red lactic acid.
Background
L-Lactic acid (L-Lactic acid): molecular formula C 3 H 6 O 3 The boiling point is 125 ℃,the L-lactic acid is an organic acid which is prepared by taking corn starch, raw material cane sugar, beet sugar or molasses thereof and the like as raw materials and refining the raw materials through biological fermentation, and is colorless clear viscous liquid, and an aqueous solution shows an acid reaction. Optionally mixed with water, ethanol or diethyl ether, and insoluble in chloroform. Because of the levorotatory characteristic, the compound has good biological compatibility, can be fused with mammals, can directly participate in human metabolism, has no side effect, and is widely applied to the fields of food, medicine and the like.
The L-lactic acid is prepared by saccharifying starch-containing raw materials, inoculating lactic acid strain, fermenting, and performing acidolysis, filtering, pre-concentrating, decolorizing, ion-exchange, concentrating membrane filtration, concentrating, and molecular distillation. The fermentation liquor is treated by molecular distillation to obtain a light phase and a heavy phase, and the concentrated solution produced by membrane filtration and the heavy phase produced by molecular distillation are generally called red lactic acid. Although the lactic acid concentration of the red lactic acid can be 60% or more, the red lactic acid contains impurities such as sugars, pigments, proteins, salts, and the like, and has a low utility value, and as shown in fig. 7, the chromaticity of the red lactic acid is very high. The traditional process is to mix a part of the red lactic acid back, and a part of the red lactic acid is used as waste. Since the red lactic acid contains sugars, proteins, and the like, it is not easy to store and it is difficult to handle it as a waste.
Therefore, it is necessary to purify red lactic acid by an industrial apparatus.
Disclosure of Invention
In order to improve the utilization rate of the red lactic acid, the invention provides a valve array type continuous ion exchange system for industrial production to purify the red lactic acid, which can increase the additional value of the red lactic acid, reduce the treatment amount of waste materials and realize the change of waste into valuable.
The technical scheme of the invention is as follows: a valve array type continuous ion exchange system for purifying red lactic acid comprises an adsorption zone, a desorption zone and a regeneration zone, wherein each zone comprises at least one anion exchange resin column; the feed of the anion exchange resin column in the adsorption zone is a red lactic acid solution, the anion exchange resin column in the desorption zone adsorbs lactate, the feed is a sulfuric acid solution, the anion exchange resin column in the regeneration zone adsorbs sulfate, and the feed is an ammonia water solution; and the anion exchange resin column in the adsorption zone is switched to the desorption zone after adsorbing lactate and being saturated, the lactate ions on the anion exchange resin column in the desorption zone are switched to the regeneration zone after being desorbed, and the anion exchange resin column in the regeneration zone is switched to the adsorption zone after being regenerated.
The anion exchange resin column is a weak-base anion exchange resin column.
The valve array type continuous ion exchange system is controlled to continuously operate by a PLC (programmable logic controller) in a full-automatic mode.
The valve array type continuous ion exchange system also comprises a washing material area, a washing acid area and a water leaching area, wherein the feeding materials of the washing material area, the washing acid area and the water leaching area are water; and after the regeneration of the anion exchange resin column in the regeneration area is finished, the anion exchange resin column is switched to the water leaching area to be subjected to water leaching and then switched to the adsorption area.
The valve array type continuous ion exchange system further comprises a backwashing area, the anion exchange resin column in the water washing acid area is switched to the backwashing area for resin backwashing after water washing is finished, and the anion exchange resin column is switched to the regeneration area after backwashing is finished.
The anion exchange resin column in the backwashing area is in a lower-upper-lower-row structure.
The feed of the backwashing area is water or a dilute ammonia solution which flows out by fast leaching of the first anion exchange resin column of the water leaching area.
The adsorption zone comprises 2 or more than 2 anion exchange resin columns connected in series.
The resolving area comprises 2 or more than 2 anion exchange resin columns which are connected in series.
The mass concentration of the feed of the red lactic acid solution in the adsorption zone is 10-30%.
The mass concentration of the sulfuric acid solution in the desorption zone is 10-40%.
The mass concentration of the ammonia water in the regeneration zone is 10-30%.
The ion exchange resin is acrylic weak-base anion exchange resin.
The adsorption area, the analysis area and the regeneration area are sequentially arranged, when the adsorption area is switched each time, the adsorption area is switched to the analysis area by one anion exchange resin column, the analysis area is switched to the regeneration area by one anion exchange resin column, and the regeneration area is switched to the adsorption area by one anion exchange resin column, so that the continuous valve array type ion exchange system can continuously and stably operate.
The adsorption zone, the washing material zone, the desorption zone, the washing acid zone, the backwashing zone, the regeneration zone and the water leaching zone are sequentially arranged, when resin is switched every time, the adsorption zone is switched to the washing material zone through one anion exchange resin column, the washing material zone is switched to the desorption zone through one anion exchange resin column, the desorption zone is switched to the washing acid zone through one anion exchange resin column, the washing acid zone is switched to the backwashing zone through one anion exchange resin column, the backwashing zone is switched to the regeneration zone through one anion exchange resin column, the regeneration zone is switched to the water leaching zone through one anion exchange resin column, and the water leaching zone is switched to the adsorption zone through one anion exchange resin column.
And detecting the pH value of the effluent of the last anion exchange resin column in the adsorption area, and when the pH value is less than 3, the red lactic acid solution is not added into the first anion exchange resin column in the adsorption area any more, and the anion exchange resin column is switched to the next procedure.
And detecting the sulfate radical concentration of the effluent of the last anion exchange resin column in the analysis area, and when the sulfate radical concentration is greater than a set value, the sulfuric acid solution does not enter the first anion exchange resin column of the lactate radical in the analysis area any more, and the anion exchange resin column is switched to the next working procedure.
The valve array type continuous ion exchange system for purifying the red lactic acid continuously operates by switching the resin subareas and the resin columns, utilizes the groups on the ion exchange resin to adsorb corresponding ions, namely lactate, directly separates protein, polysaccharide and salts in the red lactic acid solution from the lactic acid, extracts the lactic acid, and recovers a byproduct, namely ammonium sulfate, thereby changing waste into valuable, reducing the accumulation of a large amount of waste red lactic acid, improving the yield of the lactic acid, increasing the benefit of enterprises, protecting the environment, achieving the beneficial effects of energy conservation and environmental protection, and having important significance in environmental protection.
The consumption of acid, alkali and water is reduced by connecting a plurality of columns in series, and the switching of a functional area and the continuous operation of a system are realized by controlling a plurality of valves.
Drawings
Fig. 1 is a schematic structural diagram of a valve array type continuous ion exchange system for purification of red lactic acid of example 1.
Fig. 2 is a schematic structural diagram of a valve array type continuous ion exchange system for purification of red lactic acid of example 2.
FIG. 3 is a schematic diagram of the structure of a valve-matrix continuous ion-exchange system for purification of red lactic acid according to example 3.
FIG. 4 is a schematic diagram of the structure of a valve-matrix continuous ion-exchange system for purification of red lactic acid of example 4.
FIG. 5 is a schematic diagram of the structure of a valve array type continuous ion exchange system for purification of red lactic acid of example 5.
FIG. 6 is a schematic diagram of the structure of a valve matrix type continuous ion exchange system for purification of red lactic acid of example 6.
FIG. 7 is a schematic diagram of the red lactic acid starting material used in example 6.
Figure 8 is a physical comparison of the product prepared using the system of example 6 with a solution of lactic acid red into a valve matrix continuous ion exchange system.
Detailed Description
The present invention will be described in detail with reference to the following examples and drawings.
The red lactic acid is a heavy phase product obtained by molecular distillation in the process of preparing lactic acid from lactic acid fermentation liquor and/or a concentrated solution obtained by membrane filtration, and contains a small amount of impurities such as sugar, pigment, protein, salt and the like besides lactic acid. The mass concentration of lactic acid in the red lactic acid is 30-70%. Before the valve array type continuous ion exchange system is adopted to treat the red lactic acid, the red lactic acid is subjected to pretreatment such as dilution, acidolysis and decoloration. The red lactic acid is diluted with pure water. Diluting the red lactic acid, and carrying out acidolysis by using concentrated sulfuric acid, wherein the amount of the sulfuric acid solution is 1-5 per mill of the feeding mass of the red lactic acid solution, and the concentration of the sulfuric acid solution is 98%. The decolorization can be carried out by adopting activated carbon decolorization plate-and-frame filtration.
Example 1
As shown in figure 1, a valve array type continuous ion exchange system for purifying red lactic acid comprises an adsorption zone 1, a desorption zone 2 and a regeneration zone 3, wherein each zone comprises an anion exchange resin column; the feeding material of the anion exchange resin column of the adsorption area 1 is a red lactic acid solution, the anion exchange resin column of the desorption area 2 adsorbs lactate, the feeding material is a sulfuric acid solution, the anion exchange resin column of the regeneration area 3 adsorbs sulfate, and the feeding material is an ammonia water solution; the anion exchange resin column of the adsorption zone 1 is saturated to adsorb lactate and then is switched to the desorption zone 2, the lactate ions on the anion exchange resin column of the desorption zone 2 are switched to the regeneration zone 3 after being desorbed, and the anion exchange resin column of the regeneration zone 3 is switched to the adsorption zone 1 after being regenerated. The valve array type continuous ion exchange system is controlled to continuously operate by a PLC (programmable logic controller) in a full-automatic mode. The ion exchange resin in the system is weak-base acrylic anion exchange resin.
The operation method of the valve array type multi-unit continuous ion exchange system comprises the following steps:
(1) feeding a solution of the red lactic acid at a temperature of 30-40 ℃ into an anion exchange resin column of the adsorption zone 1; the red lactic acid solution is waste red lactic acid generated in the process of producing lactic acid by fermentation and refining, is diluted, is subjected to acidolysis, is decolorized by active carbon and is filtered by a plate frame to obtain filtrate, and the feeding mass concentration of the red lactic acid solution is 10 percent;
(2) using a normal-temperature dilute sulfuric acid solution as an analysis agent, and analyzing the lactic acid adsorbed by the anion exchange resin column in the analysis area 2 to obtain a refined lactic acid solution, wherein the concentration of the fed dilute sulfuric acid solution is 15%;
(3) and (3) regenerating the resin in the anion exchange resin column in the regeneration zone 3 by using a normal-temperature dilute ammonia solution as a regenerant to obtain an ammonium sulfate solution and a regenerated anion exchange resin column, wherein the mass concentration of the ammonia water is 20%.
Example 2
As shown in figure 2, a valve array type continuous ion exchange system for purifying red lactic acid comprises an adsorption zone 1, a desorption zone 2 and a regeneration zone 3, wherein each zone comprises two anion exchange resin columns; the feeding of the anion exchange resin column of the adsorption zone 1 is a red lactic acid solution, the anion exchange resin column of the desorption zone 2 adsorbs lactate, the feeding is a sulfuric acid solution, the anion exchange resin column of the regeneration zone 3 adsorbs sulfate, and the feeding is an ammonia water solution; the anion exchange resin column of the adsorption zone 1 is saturated to adsorb lactate and then is switched to the desorption zone 2, the lactate ions on the anion exchange resin column of the desorption zone 2 are switched to the regeneration zone 3 after being desorbed, and the anion exchange resin column of the regeneration zone 3 is switched to the adsorption zone 1 after being regenerated. The valve array type continuous ion exchange system is controlled to continuously operate by a PLC (programmable logic controller) in a full-automatic mode. The ion exchange resin in the system is weak-base acrylic anion exchange resin.
The operation method of the valve array type multi-unit continuous ion exchange system comprises the following steps:
(1) feeding the red lactic acid solution with the temperature of 40-60 ℃ into an anion exchange resin column of the adsorption zone 1; the red lactic acid solution is waste red lactic acid generated in the process of producing lactic acid by fermentation and refining, is diluted, is subjected to acidolysis, is decolorized by active carbon and is filtered by a plate frame to obtain filtrate, and the feeding mass concentration of the red lactic acid solution is 25 percent;
(2) using a normal-temperature dilute sulfuric acid solution as an analysis agent, and analyzing the lactic acid adsorbed by the anion exchange resin column in the analysis area 2 to obtain a refined lactic acid solution, wherein the mass concentration of the fed dilute sulfuric acid solution is 10%;
(3) and (3) regenerating the resin in the anion exchange resin column in the regeneration zone 3 by using a normal-temperature dilute ammonia solution as a regenerant to obtain an ammonium sulfate solution and a regenerated anion exchange resin column, wherein the mass concentration of ammonia is 25%.
Example 3
As shown in figure 3, a valve array type continuous ion exchange system for purifying red lactic acid comprises an adsorption zone 1, a resolution zone 2 and a regeneration zone 3, wherein each zone comprises more than two anion exchange resin columns; the feeding of the anion exchange resin column of the adsorption zone 1 is a red lactic acid solution, the anion exchange resin column of the desorption zone 2 adsorbs lactate, the feeding is a sulfuric acid solution, the anion exchange resin column of the regeneration zone 3 adsorbs sulfate, and the feeding is an ammonia water solution; the anion exchange resin column of the adsorption zone 1 is saturated to adsorb lactate and then is switched to the desorption zone 2, the lactate ions on the anion exchange resin column of the desorption zone 2 are switched to the regeneration zone 3 after being desorbed, and the anion exchange resin column of the regeneration zone 3 is switched to the adsorption zone 1 after being regenerated. The valve array type continuous ion exchange system is controlled to continuously operate by a PLC (programmable logic controller) in a full-automatic mode. The ion exchange resin in the system is weak-base acrylic anion exchange resin.
The operation method of the valve array type multi-unit continuous ion exchange system comprises the following steps:
(1) feeding a solution of the red lactic acid at a temperature of 60-80 ℃ into an anion exchange resin column of the adsorption zone 1; the red lactic acid solution is waste red lactic acid generated in the process of producing lactic acid by fermentation and refining, is diluted, is subjected to acidolysis, is decolorized by active carbon and is filtered by a plate frame to obtain filtrate, and the feeding mass concentration of the red lactic acid solution is 30%;
(2) using a normal-temperature dilute sulfuric acid solution as an analysis agent, and analyzing the lactic acid adsorbed by the anion exchange resin column in the analysis area 2 to obtain a refined lactic acid solution, wherein the concentration of the fed dilute sulfuric acid solution is 40%;
(3) and (3) regenerating the resin in the anion exchange resin column in the regeneration zone 3 by using a normal-temperature dilute ammonia solution as a regenerant to obtain an ammonium sulfate solution and a regenerated anion exchange resin column, wherein the mass concentration of ammonia is 30%.
Example 4
As shown in fig. 4, a valve array type continuous ion exchange system for purifying red lactic acid comprises an adsorption area 1, a desorption area 2, a regeneration area 3, a water washing material area 4, a water acid washing area 5, a water leaching area 6 and a backwashing area 7, wherein each area is provided with an anion exchange resin column; the feeding of the anion exchange resin column of the adsorption area 1 is a red lactic acid solution, the anion exchange resin column of the analysis area 2 adsorbs lactate, the feeding is a sulfuric acid solution, the anion exchange resin column of the regeneration area 3 adsorbs sulfate radicals, the feeding is an ammonia water solution, the water washing material area 4, the water washing acid area 5 and the water leaching area 6 all feed water, and the feeding of the backwashing area 7 is water.
When the resin columns are switched every time, the adsorption area 1 is switched to the water washing material area 4 through one anion exchange resin column, the water washing material area 4 is switched to the analysis area 2 through one anion exchange resin column, the analysis area 2 is switched to the water washing acid area 5 through one anion exchange resin column, the water washing acid area 5 is switched to the backwashing area 7 through one anion exchange resin column, the backwashing area 7 is switched to the regeneration area 3 through one anion exchange resin column, the regeneration area 3 is switched to the water washing area 6 through one anion exchange resin column, the water washing area 6 is switched to the adsorption area 1 through one anion exchange resin column, and the valve array type continuous ion exchange system runs continuously. The valve array type continuous ion exchange system is controlled to continuously operate by a PLC (programmable logic controller) in a full-automatic mode. The ion exchange resin in the system is weak-base acrylic anion exchange resin.
The operation method of the valve array type multi-unit continuous ion exchange system comprises the following steps:
(1) feeding a solution of the red lactic acid at a temperature of 50-70 ℃ into an anion exchange resin column of the adsorption zone 1; the red lactic acid solution is waste red lactic acid generated in the process of producing lactic acid by fermentation and refining, is diluted, is subjected to acidolysis, is decolorized by active carbon and is filtered by a plate frame to obtain filtrate, and the feeding mass concentration of the red lactic acid solution is 15%;
(2) eluting the residual red lactic acid solution in the anion exchange resin column of the water washing material zone 4 by using the evaporated condensate water or the steam condensate water or the deionized water as an eluent, and refluxing the eluent to the crude lactic acid tank;
(3) using normal temperature dilute sulfuric acid solution as resolving agent, resolving lactic acid adsorbed by anion exchange resin column in resolving area 2 to obtain resolving liquid as refined lactic acid solution, wherein the concentration of dilute sulfuric acid solution is 20%;
(4) washing an anion exchange resin column in the water washing acid zone 5 by using the evaporated condensate water or the steam condensate water or the deionized water as a feed material, and washing out the residual sulfuric acid solution;
(5) backwashing the anion exchange resin column switched to the backwashing area 7, and switching the anion exchange resin column of the backwashing area 7 from the water washing acid area 5;
(6) regenerating the anion exchange resin column in the regeneration zone 3 by using a normal-temperature dilute ammonia solution as a regenerant to obtain an ammonium sulfate solution and a regenerated anion exchange resin column, wherein the mass concentration of ammonia is 15%;
(7) and (3) cleaning the anion exchange resin column of the water leaching area 6 by taking the evaporated condensate water or the steam condensate water or the deionized water as a feeding material, washing out the residual ammonia water solution, and switching to the adsorption area 1 for another period of operation after the anion exchange resin column of the water leaching area 6 is leached.
Example 5
As shown in fig. 5, a valve array type continuous ion exchange system for purifying red lactic acid comprises an adsorption area 1, an analysis area 2, a regeneration area 3, a water washing material area 4, a water washing acid area 5, a water leaching area 6 and a backwashing area 7, wherein the adsorption area 1, the analysis area 2, the regeneration area 3, the water washing material area 4, the water washing acid area 5 and the water leaching area 6 are all provided with two anion exchange resin columns, and the backwashing area 7 is provided with 1 resin column; the feeding of the anion exchange resin column of the adsorption area 1 is a red lactic acid solution, the anion exchange resin column of the analysis area 2 adsorbs lactate, the feeding is a sulfuric acid solution, the anion exchange resin column of the regeneration area 3 adsorbs sulfate radicals, the feeding is an ammonia water solution, the water washing material area 4, the water washing acid area 5 and the water leaching area 6 all feed water, and the feeding of the backwashing area 7 is water.
When the resin columns are switched every time, the adsorption area 1 is switched to the water washing material area 4 through one anion exchange resin column, the water washing material area 4 is switched to the analysis area 2 through one anion exchange resin column, the analysis area 2 is switched to the water washing acid area 5 through one anion exchange resin column, the water washing acid area 5 is switched to the backwashing area 7 through one anion exchange resin column, the backwashing area 7 is switched to the regeneration area 3 through one anion exchange resin column, the regeneration area 3 is switched to the water washing area 6 through one anion exchange resin column, the water washing area 6 is switched to the adsorption area 1 through one anion exchange resin column, and the valve array type continuous ion exchange system runs continuously. The valve array type continuous ion exchange system is controlled to continuously operate by a PLC (programmable logic controller) in a full-automatic mode. The ion exchange resin in the system is weak-base acrylic anion exchange resin.
The operation method of the valve array type multi-unit continuous ion exchange system comprises the following steps:
(1) feeding a solution of the red lactic acid at a temperature of 0-30 ℃ into an anion exchange resin column of the adsorption zone 1; the red lactic acid solution is waste red lactic acid generated in the process of producing lactic acid by fermentation and refining, is diluted, is subjected to acidolysis, is decolorized by active carbon and is filtered by a plate frame to obtain filtrate, and the feed mass concentration of the red lactic acid solution is 20%;
(2) eluting the residual red lactic acid solution in the anion exchange resin column of the water washing material zone 4 by using the evaporated condensate water or the steam condensate water or the deionized water as an eluent, and refluxing the eluent to the crude lactic acid tank;
(3) using a normal-temperature dilute sulfuric acid solution as an analysis agent to analyze the lactic acid adsorbed by the anion exchange resin column in the analysis area 2 to obtain a refined lactic acid solution, wherein the concentration of the dilute sulfuric acid solution is 15%;
(4) washing an anion exchange resin column in the water washing acid zone 5 by using the evaporated condensate water or the steam condensate water or the deionized water as a feed material, and washing out the residual sulfuric acid solution;
(5) backwashing the anion exchange resin column switched to the backwashing area 7, and switching the anion exchange resin column of the backwashing area from the water washing acid area 5;
(6) regenerating the anion exchange resin column in the regeneration zone 3 by using a normal-temperature dilute ammonia solution as a regenerant to obtain an ammonium sulfate solution and a regenerated anion exchange resin column, wherein the mass concentration of ammonia is 10%;
(7) and (3) cleaning the anion exchange resin column of the water leaching area 6 by taking the evaporated condensate water or the steam condensate water or the deionized water as a feeding material, washing out the residual ammonia water solution, and switching to the adsorption area 1 for another period of operation after the anion exchange resin column of the water leaching area 6 is leached.
Example 6
As shown in fig. 6, a valve array type continuous ion exchange system for purifying red lactic acid comprises an adsorption area 1, a desorption area 2, a regeneration area 3, a water washing material area 4, a water washing acid area 5, a water washing area 6 and a backwashing area 7; the feeding of the anion exchange resin column of the adsorption area 1 is a red lactic acid solution, the anion exchange resin column of the analysis area 2 adsorbs lactate, the feeding is a sulfuric acid solution, the anion exchange resin column of the regeneration area 3 adsorbs sulfate radicals, the feeding is an ammonia water solution, the water washing material area 4, the water washing acid area 5 and the water washing area 6 all feed water, and the feeding of the backwashing area 7 is dilute ammonia water.
The specific structure of the valve array type continuous ion exchange system for purifying the red lactic acid is as follows:
adsorption zone 1: the number of anion exchange resin columns in this zone is preferably 2 or more, and in this embodiment, the unit comprises 8 to 13#6 ion exchange columns, but the number of resin columns may be set as the case may be.
The red lactic acid solution sequentially enters the ion resin exchange columns of the adsorption zone 1 in a downstream column-string mode, and the ionic lactic acid is exchanged to the groups of the resin framework.
And (4) washing a material area: the water washing zone had 1 anion exchange resin column which was switched over from the adsorption zone 1. Specifically, the outlet of the 13# column (the last anion exchange resin column in the adsorption zone 1) is detected, when the pH value is less than 3, the 8# column is saturated by adsorption, the column cutting operation is performed at the moment, the 8# column is cut to the washing material zone 4 where the 7# column is located for washing, the residual material in the column is washed out to a red lactic acid tank, and when the 8# column is switched, the 7# column is switched to the analysis zone.
Detecting the effluent of the anion exchange resin column in the water washing material zone 4, wherein the effluent is qualified when the pH value is more than or equal to 3, and switching to the next analysis zone 2;
analysis area 2: the number of anion exchange resin columns in the desorption zone 2 is preferably more than 2, and the anion exchange resin columns in the zone are switched from the water washing material zone 4, namely, the resin columns are cut into the desorption zone 2 after the water washing material is finished. In this example, the analysis zone 2 is composed of 3 resin columns (such as column # 4-6 in FIG. 6), and the resin columns in the analysis zone 2 are all resin columns saturated by lactic acid adsorption cut one by the water wash zone 4. Sulfuric acid solution is fed from the No. 4 column and sequentially flows in the column to the No. 5 and No. 6 columns, the sulfate radicals in the column displace lactic acid on the resin, and the lactic acid is discharged from the No. 6 column to a lactic acid recovery tank, so that a required cleaner lactic acid product is obtained. And (3) taking an outlet sample of the 6# column to detect sulfate radicals, stopping feeding the sulfuric acid solution into the 4# column when the detected value of the sulfate radicals is larger than a set value, and switching the resin columns (the sulfate radicals are titrated by a barium chloride solution of 0.25g/ml, and the set value is reached when white precipitates appear).
Water washing acid zone 5: consists of 3 resin columns (as shown in figures 1-3 #) (the number of resin columns can be set according to actual conditions). The resolved column is cut into a water washing acid area 5, the residual sulfuric acid in the column is washed out by pure water, water is fed from the 1# column, the column is sequentially connected to the 2# column and the 3# column, the discharged acid is discharged from the 3# column, and the discharged acid enters a sulfuric acid tank, and the standard of water washing completion is that the pH value of the discharged water of the current column such as the 1# column is more than 3.5.
A backwashing zone 7: contains 20# of the one column. And after the anion exchange resin column in the water washing acid zone 5 finishes water washing, switching to a backwashing zone 7 for backwashing.
The backwashing area can be independently supplied with water, dilute ammonia water generated when the 14# column in the water leaching area 6 is quickly leached can be connected to the 20# column through a backwashing inlet valve in series, the anion exchange resin columns in the backwashing area are of a lower-inlet-upper-outlet structure, impurities in the columns are washed out, and the discharged water is clear.
Regeneration zone 3: the acid district is washed to water and the post that the water washing was accomplished in the post or the backwash district of accomplishing the backwash cuts into the regeneration zone, and the regeneration zone contains 3 posts 17-19# post (can set up the quantity of resin column according to actual conditions), advances weak aqueous ammonia by 17# post, and the cluster is to 18#, 19# post in proper order, and the aqueous ammonia replaces the exchange capacity of recovering the resin with the sulfate radical on the resin, and sulfate radical and ammonia radical combination formation ammonium sulfate are discharged to the ammonium sulfate jar by 19# post.
A water leaching area 6: comprises 3 resin columns, namely 14-16# columns. The resin columns regenerated in the regeneration zone 3 are sequentially transferred into a water spraying zone 6, deionized water is fed from a 14# column and sequentially flows to a 15# column and a 16# column, and the deionized water is discharged from the 16# column. The standard for completion of the elution is that the pH of the effluent from the current column, e.g., column # 14, is < 10 and the anion exchange resin column after completion of the elution is switched to adsorption zone 1. The discharged water is recycled to the ammonia water tank.
The flow speed of the leaching water in the leaching area is 5-8 BV/h.
When the system runs, all the zones run the parameters set by each zone simultaneously, one resin column is switched every period, one resin column is cut out from one zone, and one resin column is cut in from the adjacent zone, so that the reciprocating circulation realizes the continuous running.
The operation method of the valve array type multi-unit continuous ion exchange system comprises the following steps:
(1) feeding a solution of the red lactic acid at a temperature of 30-40 ℃ into a weak base anion exchange resin column of the adsorption zone 1; as shown in fig. 7, the concentration of lactic acid is about 60%, the red lactic acid is diluted and subjected to acidolysis, decolorized by activated carbon and filtered by a plate frame to obtain a filtrate which is a red lactic acid solution, and the feed mass concentration of the red lactic acid solution is 25.6%; the object is shown in figure 8 as the first bottle.
(2) Eluting the residual red lactic acid solution in the anion exchange resin column of the water washing material zone 4 by using the evaporated condensate water or the steam condensate water or the deionized water as an eluent, and refluxing the eluent to the crude lactic acid tank;
(3) using a normal-temperature dilute sulfuric acid solution as an analysis agent to analyze the lactic acid adsorbed by the anion exchange resin column in the analysis area 2 to obtain a refined lactic acid solution, wherein the concentration of the dilute sulfuric acid solution is 25%;
(4) washing an anion exchange resin column in the water washing acid zone 5 by using the evaporated condensate water or the steam condensate water or the deionized water as a feed material, and washing out the residual sulfuric acid solution;
(5) backwashing the anion exchange resin column switched to the backwashing area 7, and switching the anion exchange resin column of the backwashing area from the water washing acid area 5;
(6) regenerating the anion exchange resin column in the regeneration zone 3 by using a normal-temperature dilute ammonia solution as a regenerant to obtain an ammonium sulfate solution and a regenerated anion exchange resin column, wherein the mass concentration of ammonia is 20%;
(7) and (3) cleaning the anion exchange resin column of the water leaching area 6 by taking the evaporated condensate water or the steam condensate water or the deionized water as a feeding material, washing out the residual ammonia water solution, and switching to the adsorption area 1 for another period of operation after the anion exchange resin column of the water leaching area 6 is leached.
Discharge detection indexes are as follows: the concentration of the analysis solution (lactic acid) is 10-18%, the sulfate radical content is 0, and the chroma is 400-500 APHA; the concentration of the byproduct ammonium sulfate is 6-8%. A comparison of the red lactic acid solution with the lactic acid solution after treatment with the valve array type continuous ion exchange system is shown in FIG. 8. The material liquid filled in the bottle with the label of fig. 8 as the red lactic acid is the filtrate obtained by diluting the red lactic acid raw material, decoloring by active carbon and filtering by a plate frame, although the chroma is reduced, compared with the red lactic acid raw material in fig. 7, the color change can not be seen by naked eyes, which shows that although the impurity content is very high after the decoloring treatment by the active carbon, the product with the label of fig. 8 as the recovered lactic acid can be obtained after the treatment of the valve array type multi-unit continuous ion exchange system, and the liquid is clear and transparent and meets the requirement of refined lactic acid. Therefore, the invention solves the important problem that the red milk has high acid content but cannot be utilized due to a large amount of pigment and impurities, and generates great economic benefit and environmental benefit.
TABLE 1 comparison of pre-and post-red lactic acid indices for the system of example 6
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. A valve array type continuous ion exchange system for purifying red lactic acid is characterized by comprising an adsorption zone, a desorption zone and a regeneration zone, wherein each zone comprises at least one anion exchange resin column; the feed of the anion exchange resin column in the adsorption zone is a red lactic acid solution; the red lactic acid solution is waste red lactic acid generated in the process of producing lactic acid by fermentation refining, the filtrate is obtained after dilution and acidolysis, decolorization is carried out by active carbon and plate-frame filtration, the red lactic acid is diluted by pure water, and acidolysis is carried out by a concentrated sulfuric acid solution with the concentration of 98 percent after dilution; adsorbing lactate on an anion exchange resin column in the analysis area, wherein the fed material is a sulfuric acid solution, adsorbing sulfate on an anion exchange resin column in the regeneration area, and feeding the material is an ammonia water solution to obtain an ammonium sulfate solution; and the anion exchange resin column in the adsorption zone is switched to the desorption zone after adsorbing lactate and being saturated, the lactate ions on the anion exchange resin column in the desorption zone are switched to the regeneration zone after being desorbed, and the anion exchange resin column in the regeneration zone is switched to the adsorption zone after being regenerated.
2. The valve array type continuous ion exchange system according to claim 1, further comprising a material washing zone, an acid washing zone and a water leaching zone, wherein the materials fed into the material washing zone, the acid washing zone and the water leaching zone are water, the anion exchange resin column in the adsorption zone is switched to the material washing zone after being saturated in adsorption and then switched to the desorption zone after being washed with water, the anion exchange resin column in the desorption zone is switched to the acid washing zone after being washed with water after being resolved with lactic acid, and then switched to the regeneration zone, and the anion exchange resin column in the regeneration zone is switched to the water leaching zone after being regenerated and then switched to the adsorption zone after being washed with water.
3. The valve array type continuous ion exchange system according to claim 2, wherein the valve array type continuous ion exchange system further comprises a backwashing area, the anion exchange resin column in the water washing acid area is switched to the backwashing area for resin backwashing after water washing is completed, and the anion exchange resin column is switched to the regeneration area after backwashing is completed.
4. The valve array continuous ion exchange system according to any one of claims 1-3, wherein the valve array continuous ion exchange system is operated continuously by PLC full-automatic control.
5. The valve matrix continuous ion exchange system of claim 3, wherein the anion exchange resin columns in the back washing zone are in a lower-to-upper row structure.
6. The valve matrix continuous ion exchange system according to claim 1, wherein the adsorption zone comprises 2 or more than 2 anion exchange resin columns connected in series; the resolving area comprises 2 or more than 2 anion exchange resin columns which are connected in series.
7. The valve array type continuous ion exchange system according to claim 1, wherein the adsorption zone, the desorption zone and the regeneration zone are arranged in sequence, and each time switching is performed, the adsorption zone switches one anion exchange resin column to the desorption zone, the desorption zone switches one anion exchange resin column to the regeneration zone, and the regeneration zone switches one anion exchange resin column to the adsorption zone.
8. The valve array type continuous ion exchange system according to claim 3, wherein the adsorption zone, the water wash material zone, the desorption zone, the water wash acid zone, the backwashing zone, the regeneration zone and the water rinsing zone are arranged in sequence, each time the resin is switched, the adsorption zone switches one anion exchange resin column to the water wash material zone, the water wash material zone switches one anion exchange resin column to the desorption zone, the desorption zone switches one anion exchange resin column to the water wash acid zone, the water wash acid zone switches one anion exchange resin column to the backwashing zone, the backwashing zone switches one anion exchange resin column to the regeneration zone, the regeneration zone switches one anion exchange resin column to the water rinsing zone, and the water rinsing zone switches one anion exchange resin column to the adsorption zone.
9. The valve array type continuous ion exchange system according to any one of claims 1 to 3, wherein the pH value of the effluent of the last anion exchange resin column in the adsorption zone is detected, and when the pH value is less than 3, the red lactic acid solution is not added to the first anion exchange resin column in the adsorption zone, and the anion exchange resin column is switched to the next process.
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