LU505449A1 - Sucrose decoloring method and system - Google Patents
Sucrose decoloring method and system Download PDFInfo
- Publication number
- LU505449A1 LU505449A1 LU505449A LU505449A LU505449A1 LU 505449 A1 LU505449 A1 LU 505449A1 LU 505449 A LU505449 A LU 505449A LU 505449 A LU505449 A LU 505449A LU 505449 A1 LU505449 A1 LU 505449A1
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- Luxembourg
- Prior art keywords
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- anion resin
- resin column
- regeneration
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- 238000000034 method Methods 0.000 title claims abstract description 163
- 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 title claims abstract description 58
- 229930006000 Sucrose Natural products 0.000 title claims abstract description 58
- 239000005720 sucrose Substances 0.000 title claims abstract description 58
- 239000011347 resin Substances 0.000 claims abstract description 313
- 229920005989 resin Polymers 0.000 claims abstract description 313
- 230000008569 process Effects 0.000 claims abstract description 146
- 230000008929 regeneration Effects 0.000 claims abstract description 99
- 238000011069 regeneration method Methods 0.000 claims abstract description 99
- 235000009508 confectionery Nutrition 0.000 claims abstract description 67
- 238000011001 backwashing Methods 0.000 claims abstract description 57
- 150000001450 anions Chemical class 0.000 claims description 108
- 238000004042 decolorization Methods 0.000 claims description 101
- -1 acrylic anion Chemical class 0.000 claims description 99
- 239000000243 solution Substances 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 33
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 22
- 239000011780 sodium chloride Substances 0.000 claims description 11
- 239000011259 mixed solution Substances 0.000 claims description 10
- 230000001172 regenerating effect Effects 0.000 claims description 2
- 230000000630 rising effect Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 6
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 230000000052 comparative effect Effects 0.000 description 26
- 239000000463 material Substances 0.000 description 9
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 8
- 229910001415 sodium ion Inorganic materials 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 239000012267 brine Substances 0.000 description 6
- 239000000049 pigment Substances 0.000 description 6
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 5
- 238000001514 detection method Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 238000006386 neutralization reaction Methods 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 230000009467 reduction Effects 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 2
- 150000002500 ions Chemical group 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- DEXFNLNNUZKHNO-UHFFFAOYSA-N 6-[3-[4-[2-(2,3-dihydro-1H-inden-2-ylamino)pyrimidin-5-yl]piperidin-1-yl]-3-oxopropyl]-3H-1,3-benzoxazol-2-one Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C1CCN(CC1)C(CCC1=CC2=C(NC(O2)=O)C=C1)=O DEXFNLNNUZKHNO-UHFFFAOYSA-N 0.000 description 1
- 239000004925 Acrylic resin Substances 0.000 description 1
- 229920000178 Acrylic resin Polymers 0.000 description 1
- 238000013494 PH determination Methods 0.000 description 1
- 240000000111 Saccharum officinarum Species 0.000 description 1
- 235000007201 Saccharum officinarum Nutrition 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000003957 anion exchange resin Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 238000010309 melting process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/14—Purification of sugar juices using ion-exchange materials
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/14—Purification of sugar juices using ion-exchange materials
- C13B20/146—Purification of sugar juices using ion-exchange materials using only anionic ion-exchange material
-
- 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
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/50—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents
- B01J49/57—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents for anionic exchangers
-
- 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
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/60—Cleaning or rinsing ion-exchange beds
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/14—Purification of sugar juices using ion-exchange materials
- C13B20/144—Purification of sugar juices using ion-exchange materials using only cationic ion-exchange material
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K13/00—Sugars not otherwise provided for in this class
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K13/00—Sugars not otherwise provided for in this class
- C13K13/002—Xylose
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Ion Exchange (AREA)
- Saccharide Compounds (AREA)
Abstract
A sucrose decoloring method and system. The method comprises the following steps: (1) a decoloring process; (2) a sweet off process; (3) a backwashing process; (4) a regeneration process; and (5) a rinsing process. The sucrose decoloring system comprises a decoloring area, a sweet off area, a backwashing area, a regeneration area, and a rinsing area. According to the sucrose decoloring method and system of the present invention, the advantages of two different resins are fully utilized, the better decoloring effect is achieved, the decolored color value is decreased to 150IU or below from 1,200IU before decoloring, the decoloring rate is up to 85% or above, and meanwhile, the resin utilization rate is high and the resin dosage can be saved.
Description
Sucrose decoloring method and system LU505449
The present invention relates to sucrose processing technology, in particular to a method and a system for sucrose decolorization.
At present, in the sucrose refining production process using sugarcane as raw material, in order to increase the yield, the mother liquor separated from crystallization is repeatedly returned to a point before juice saturation for reuse, so that the chromatic value of the material before crystallization becomes higher and higher, which seriously affects the color quality of crystal products. In the traditional production process of sucrose decolorization, it is generally adopted to add activated carbon after juice saturation to remove pigments by decolorization and filtration.
However, due to the high pigment content in the mother liquor, and the higher chromatic value of material due to repeated reuse, the decolorization effect of activated carbon is poor, and the decolorization rate can only reach 50% to 60%, and even by decolorization using activated carbon, the chromatic value of material is still as high as around 1200IU. Some manufacturers also use fixed bed resin for decolorization, but the amount of resin used is large, the utilization rate is low, and the decolorization rate is not desired.
Contents of the present invention
In order to solve the problem of poor sucrose decolorization effect in the prior art, the present invention adopts a multi-unit continuous decolorization process to perform two-stage decolorization, thereby achieving better decolorization effect.
The present invention provides a method for sucrose decolorization, comprising the following processes: (1) Decolorization process: after feeding a sucrose solution into a plurality of acrylic anion resin columns arranged in parallel, feeding an effluent thereof into a plurality of styrenic anion resin columns arranged in parallel, thereby performing two-stage decolorization; (2) Sweet off process: by using water carrying out sweet off process in an acrylic anion resin column and a styrenic anion resin column switched from the decolorization process, and the replaced material is recovered; (3) Backwashing process: by using water backwashing an acrylic anion resin column and a 1 IEC232028PCT styrenic anion resin column switched from the sweet off process;
LU505449 (4) Regeneration process: by using a regeneration solution regenerating an acrylic anion resin column and a styrenic anion resin column switched from the backwashing process, wherein the regeneration solution is a mixed solution of NaCl and NaOH, (5) Rinsing process: by using water rinsing an acrylic anion resin column and a styrenic anion resin column switched from the regeneration process;
Wherein, the acrylic anion resin columns and the styrenic anion resin columns in the decolorization process, sweet off process, backwashing process, regeneration process, and rinsing process are switched according to the sequence of processes.
The decolorization process, sweet off process, regeneration process, and rinsing process each has two or more resin columns, and the backwashing process has one or more resin columns.
In each of the decolorization process, sweet off process, backwashing process, regeneration process and rinsing process, the acrylic anion resin columns are arranged adjacently to from an acrylic anion resin column unit, and the styrenic anion resin columns are arranged adjacently to form a styrenic anion resin column unit; in each of the sweet off process, backwashing process, regeneration process and rinsing process, the acrylic anion resin column unit and the styrenic anion resin column unit are arranged in parallel, and the same kind of resin columns are switched correspondingly when switching. For example, an acrylic anion resin column in the previous process is switched to an acrylic anion resin column unit in the next process, and a styrenic anion resin column in the previous process is switched to a styrenic anion resin column unit in the next process. In such arrangement, the decolorization process, sweet off process, backwashing process, regeneration process and rinsing process each has two or more resin columns, and each process has two kinds of resin columns at the same time.
In each of the decolorization process, sweet off process, backwashing process, regeneration process and rinsing process, the acrylic anion resin columns and the styrenic anion resin columns are arranged alternatively, and switched according to the order of the process positions where the resin columns are located when switching. Since the two kinds of resin columns are arranged alternatively, taking the procedure of switching from the decolorization process to the sweet off process as an example, the first column of the decolorization process is an acrylic anion resin column when switching, and the acrylic anion resin column is switched to the sweet off process after switching, while the adjacent styrenic anion resin column is switched to the first process position; and when switching again, the styrenic anion resin column is switched to the sweet off process. In such setting, the decolorization process, sweet off process, regeneration process and 2 IEC232028PCT rinsing process each have two or more resin columns, and have two kinds of resin columns at the
LU505449 same time; while the backwashing process can have one or more resin columns, and when there is only one resin column, the kind of resin column varies for each switching cycle.
For the setting of resin columns arranged alternatively, in the regeneration process, in one switching cycle, the regeneration solution only regenerates one kind of resin column, and in the next switching cycle, it regenerates another kind of resin column.
The sucrose solution in the decolorization process has a temperature of 70 to 80 °C, and a sucrose mass percentage concentration of 50 to 55 %.
The regeneration solution is a mixed solution of a NaCl solution with a mass percentage concentration of 8 to 10 % and a NaOH solution with a mass percentage concentration of 0.5 to 1.0 %.
When the sweet off process has an effluent with a sucrose mass percentage concentration of > 25%, the effluent is returned to a feed tank; when the effluent has a sucrose mass percentage concentration of < 25%, the effluent is returned to a sweet water tank.
When the regeneration process has an effluent with a sodium ion concentration of <2%, the effluent undergoes wastewater treatment, and when the sodium ion concentration is > 2%, the effluent is recovered.
When the rinsing process has an effluent with a sodium ion concentration of > 2%, the effluent is recovered, and when the sodium ion concentration is < 2%, the effluent undergoes wastewater treatment.
The present invention provides a system for sucrose decolorization, comprising:
Decolorization section: it comprises an acrylic anion resin column unit and a styrenic anion resin column unit, the acrylic anion resin column unit and the styrenic anion resin column unit are connected in series, the acrylic anion resin column unit comprises a plurality of acrylic anion resin columns connected in parallel, the styrenic anion resin column unit comprises a plurality of styrenic anion resin columns connected in parallel, and the decolorization section has an influent of sucrose solution;
Sweet off section: it comprises an acrylic anion resin column and a styrenic anion resin column switched from the decolorization section, and the sweet off section has an influent of water;
Backwashing section: it comprises an acrylic anion resin column and a styrenic anion resin column switched from the sweet off section, and the backwashing section has an influent of water; 3 IEC232028PCT
Regeneration section: it comprises an acrylic anion resin column and a styrenic anion resin column switched from the backwashing section, and the regeneration section has an influent that 505449 is a mixed solution of NaCl and NaOH;
Rinsing section: it comprises an acrylic anion resin column and a styrenic anion resin column switched from the regeneration section, and the rinsing section has an influent of water;
Wherein, the acrylic anion resin columns and styrenic anion resin columns in the decolorization section, sweet off section, backwashing section, regeneration section, and rinsing section are switched according to the sequence of processes.
The decolorization section, sweet off section, regeneration section, and rinsing section each has two or more resin columns, and the backwashing section has one or more resin columns.
In each of the decolorization section, sweet off section, backwashing section, regeneration section and rinsing section, the acrylic anion resin columns are adjacently arranged to form an acrylic anion resin column unit, and the styrenic anion resin columns are adjacently arranged to form a styrenic anion resin column unit, the acrylic anion resin column unit and the styrenic anion resin column unit in the sweet off section, backwashing section, regeneration section and rinsing section are arranged in parallel, and the same kind of resin columns are switched correspondingly when switching. The decolorization section, sweet off section, backwashing section, regeneration section and rinsing section each has two or more resin columns, and each section has two kinds of resin columns.
In each of the decolorization section, sweet off section, backwashing section, regeneration section and rinsing section, the acrylic anion resin columns and styrenic anion resin columns are arranged alternatively, and switched according to the order of the process positions where the resin columns are located when switching. The decolorization section, sweet off section, regeneration section and rinsing section each has two or more resin columns, and each section has two kinds of resin columns. When one resin column is set in the backwashing section, the kind of resin column in the backwashing section is alternatively changed according to the switching cycle.
In one switching cycle, only one kind of resin column in the regeneration section is communicated with an inlet pipe of the regeneration solution, and in the next switching cycle, another kind of resin column in the regeneration section is communicated with an inlet pipe of the regeneration solution.
The last resin column in the rinsing section is connected in series with the same kind of resin column in the regeneration section. 4 IEC232028PCT
The acrylic anion resin columns and the styrenic anion resin columns in the sucrose
LU505449 decolorization system are small columns with a column diameter of 800mm to 1400mm. This column diameter range is for production in large scale.
The present invention has obtained following beneficial effects: 1. It has high utilization rate of resins, which saves resin consumption; 2. It makes full use of the advantages of two different kinds of resins (the acrylic resin has a large pigment exchange capacity; and the styrene resin has a wide range of pigment adsorption selection), and achieves better decolorization effect. After decolorization, the chromatic value 1s reduced from 1200IU before decolorization to below 150IU, the decolorization rate is as high as 85% or more; 3. The sweet off process, rinsing process, regeneration process are performed in columns arranged in series, which reduces water consumption and regeneration agent consumption, and saves more than 50% of water; 4. During regeneration process, the brine (salt-containing waste liquid discharged from the regeneration process) is recovered, and reused after membrane filtration treatment, thereby saving more than 70% of the regeneration agent; 5. The rinsing process and the regeneration process adopt same kind of resin columns arranged in series, which reduces the mutual pollution and improves the treatment effect; 6. The sweet water is used to elute a column in the sucrose decalcification process; the backwashed water is reused in the sugar melting process, which greatly reduces the discharge of wastewater. 7. The sucrose decolorization system allows continuous feeding and discharging, continuous elution, and continuous regeneration, which can be fully automatic without manual operation.
Figure 1 shows a schematic flow diagram of the sucrose decolorization method of the present invention.
Figure 2 shows a process flow diagram of the sucrose decolorization method of Example 1.
Figure 3 shows a process flow diagram of the sucrose decolorization method of Example 2 (showing cycle 1).
Figure 4 shows a process flow diagram of the sucrose decolorization method of Example 2 5 IEC232028PCT
(showing cycle 2 after switching).
LU505449
Figure 5 shows a schematic structural view of the decolorization operation set of
Comparative Example 2.
Figure 6 shows a schematic structural view of a standby set for decolorization of
Comparative Example 2.
Figure 7 shows the cycle discharge pH curves of Comparative Example 1 and Example 3.
Figure 8 shows the cycle discharge chromatic value curves of Comparative Example 1 and
Example 3.
Figure 9 shows the cycle discharge pH curves of Comparative Example 2 and Example 3.
Figure 10 shows the cycle discharge chromatic value curves of Comparative Example 2 and
Example 3.
In the figures, the acrylic anion resin columns are abbreviated as “JN”, and the styrenic anion resin columns are abbreviated as “A”.
Specific Models for Carrying Out the present invention
The embodiments of the present invention will be clearly and completely described below in conjunction with the examples and drawings. Apparently, the described examples are only some of the examples of the present invention, not all of them. The following description of at least one exemplary example is merely illustrative in nature and in no way taken as limiting the present invention, its application or uses. Based on the examples of the present invention, all other examples obtained by persons of ordinary skill in the art without creative efforts fall within the protection scope of the present invention.
A method for sucrose decolorization of the present invention comprises following processes:
Decolorization process: a sucrose solution with a mass percentage concentration of 50 to 55%, a temperature of 70 to 80°C, and a chromatic value of <1200IU is introduced into a plurality of acrylic anion resin columns arranged in parallel, then a effluent is fed into a plurality of styrenic anion resin columns arranged in parallel to undergo two-stage decolorization with a flow rate of 3BV (3 times the resin volume); the resulting effluent is checked whether it has a chromatic value of <1501U; the resulting effluent is introduced into a decolorization discharge tank and can be used in the next process;
Sweet off process: water is used to carry out sweet off process in an acrylic anion resin 6 IEC232028PCT column and a styrenic anion resin column switched from the decolorization process, and the replaced material is recovered; when the effluent has a sucrose mass percentage concentration of 505449 >25%, the effluent is returned to a decolorization feed tank; when the effluent has a sucrose mass percentage concentration of <25%, the effluent is returned to a sweet water tank, and the sweet water in the sweet water tank can be used for the sucrose decalcification process;
Backwashing process: water is used to backwash an acrylic anion resin column and a styrenic anion resin column switched from the sweet off process; the effluent of the backwashing process can be recovered to a sucrose-dissolving tank for the sugar dissolving process;
Regeneration process: a regeneration solution is used to regenerate an acrylic anion resin column and a styrenic anion resin column switched from the backwashing process, the regeneration solution is a mixed solution of a NaCl solution with a mass percentage concentration of 8 to 10% and a NaOH solution with a mass percentage concentration of 0.5 to 1.0%; when the effluent of the regeneration process has a sodium ion concentration of <2%, it enters a wastewater neutralization tank for wastewater treatment, and when the effluent has a sodium ion concentration of >2%, it is recovered to a brine recovery tank;
Rinsing process: water is used to rinse an acrylic anion resin column and a styrenic anion resin column switched from the regeneration process; when the effluent of the rinsing process has a sodium ion concentration of > 2%, it is recovered to the brine recovery tank, and when the effluent has a sodium ion concentration of <2%, it enters the wastewater neutralization tank for wastewater treatment; the liquid in the brine recovery tank undergoes membrane filtration and the filtrate is returned to a regeneration agent tank, and the concentrated residue is treated as a waste liquid;
Wherein, the acrylic anion resin columns and the styrenic anion resin columns in the decolorization process, sweet off process, backwashing process, regeneration process, and rinsing process are switched according to the sequence of processes.
Example 1 A system for sucrose decolorization, comprised:
Decolorization section: it comprised an acrylic anion resin column unit and a styrenic anion resin column unit, the acrylic anion resin column unit and the styrenic anion resin column unit were connected in series, the acrylic anion resin column unit comprised a plurality of acrylic anion resin columns connected in parallel, the styrenic anion resin column unit comprised a plurality of styrenic anion resin columns connected in parallel, and the decolorization section had an influent of sucrose solution; 7 IEC232028PCT
Sweet off section: it comprised an acrylic anion resin column and a styrenic anion resin . Lo. . . . LU505449 column switched from the decolorization section, the sweet off section had an influent of water;
Backwashing section: it comprised an acrylic anion resin column and a styrenic anion resin column switched from the sweet off section, and the backwashing section had an influent of water;
Regeneration section: it comprised an acrylic anion resin column and a styrenic anion resin column switched from the backwashing section, and the regeneration section had an influent that was a mixed solution of NaCl and NaOH;
Rinsing section: it comprised an acrylic anion resin column and a styrenic anion resin column switched from the regeneration section, and the rinsing section had an influent of water;
Wherein, the acrylic anion resin columns and the styrenic anion resin columns in the decolorization section, sweet off section, backwashing section, regeneration section, and rinsing section were switched according to the sequence of processes.
As shown in Figure 2, the acrylic anion resin columns and the styrenic anion resin columns in each of the decolorization section, sweet off section, backwashing section, regeneration section, and rinsing section were arranged separately to form independent acrylic anion resin column unit and styrenic anion resin column unit, and the resin columns of the acrylic anion resin column unit and the styrenic anion resin column unit of the previous section were switched to the next section at the same time during continuous switching. The acrylic anion resin column unit and the styrenic anion resin column unit in each of the sweet off section, backwashing section, regeneration section and rinsing section were arranged in parallel.
In each of the sweet off section, regeneration section and rinsing section, the acrylic anion resin column unit comprised a plurality of resin columns connected in series, and the styrenic anion resin column unit comprised a plurality of resin columns connected in series. The backwashing section comprised two resin columns, one of which was an acrylic anion resin column and the other was a styrenic anion resin column.
The last acrylic anion resin column in the rinsing section was connected in series with the first acrylic anion resin column in the regeneration section; and the last styrenic anion resin column in the rinsing section was connected in series with the first styrenic anion resin column in the regeneration section.
In the present example, the sucrose decolorization system could have altogether 1 to 20# acrylic anion resin columns and 1 to 20# styrenic anion resin columns, and the number of acrylic anion resin columns and the number of styrenic anion resin columns allocated in each section 8 IEC232028PCT could be determined according to the amount of sucrose processed.
LU505449
Example 2 À system for sucrose decolorization, comprised:
Decolorization section: it comprised an acrylic anion resin column unit and a styrenic anion resin column unit, the acrylic anion resin column unit and the styrenic anion resin column unit were connected in series, the acrylic anion resin column unit comprised a plurality of acrylic anion resin columns connected in parallel, the styrenic anion resin column unit comprised a plurality of styrenic anion resin columns connected in parallel, and the decolorization section had an influent of sucrose solution;
Sweet off section: it comprised an acrylic anion resin column and a styrenic anion resin column switched from the decolorization section, and the sweet off section had an influent of water;
Backwashing section: it comprised an acrylic anion resin column and a styrenic anion resin column switched from the sweet off section, and the backwashing section had an influent of water;
Regeneration section: it comprised an acrylic anion resin column and a styrenic anion resin column switched from the backwashing section, and the regeneration section had an influent that was a mixed solution of NaCl and NaOH, i.e., a mixed solution of a NaCl solution with a mass percentage concentration of 8 to 10% and a NaOH solution with a mass percentage concentration of 0.5 to 1.0%;
Rinsing section: it comprised an acrylic anion resin column and a styrenic anion resin column switched from the regeneration section, and the rinsing section had an influent of water;
Wherein, the acrylic anion resin columns and the styrenic anion resin columns in the decolorization section, sweet off section, backwashing section, regeneration section, and rinsing section were switched according to the sequence of processes.
As shown in Figure 3 and Figure 4, the acrylic anion resin columns and the styrenic anion resin columns in the decolorization section, sweet off section, backwashing section, regeneration section, and rinsing section were arranged alternatively. When switched continuously, the acrylic anion resin columns and the styrenic anion resin columns were switched to the next section in turn, and one resin column was switched each time. As shown in Figure 3, the No. 4 column in the decolorization section was an acrylic anion resin column, and the adjacent No. 5 column was a styrenic anion resin column, after switching, as shown in Figure 4, the No. 4 column was switched to the sweet off section, and the No. 5 column was switched to the process position 9 IEC232028PCT originally occupied by the No. 4 column. Each time one resin column was switched, one cycle was completed. HUS05449
The sweet off section comprised a plurality of resin columns connected in series, in which the acrylic anion resin columns and the styrenic anion resin columns were arranged alternatively and connected in series. As shown in Figure 3, the sweet off section comprised No. 1 column (styrenic anion resin column), No. 2 column (acrylic anion resin column) and No. 3 column (styrenic anion resin column), the three columns were connected in series, and water flowed through No. 1 column, No. 2 column and No. 3 column in sequence. After switching, as shown in Figure 4, the sweet off section comprised No. 2 column (acrylic anion resin column), No. 3 column (styrenic anion resin column) and No. 4 column (acrylic anion resin column), in which the No. 2 column, No. 3 column and No. 4 column were also connected in series.
The backwashing section comprised one resin column, and the resin column in the backwashing section was switched from the sweet off section, so there were different kinds of resin columns in different cycles, as shown in Figure 3, the resin column in the backwashing section at cycle 1 was No. 20 column (acrylic anion resin column). After switching, as shown in
Figure 4, the resin column in the backwashing section was No. 1 column (styrenic anion resin column).
The regeneration section comprised a plurality of resin columns, in which the acrylic anion resin columns and the styrenic anion resin columns were arranged alternatively, and the same kind of resin columns were connected in series, as shown in Figure 3, the regeneration section comprised No. 17 column (styrenic anion resin column), No. 18 column (acrylic anion resin column) and No. 19 column (styrenic anion resin column), in which the No. 17 column and No. 19 column were connected in series, and the regeneration solution flowed through the No. 17 column and No. 19 column in sequence. After switching, as shown in Figure 4, the regeneration section comprised No. 18 column (acrylic anion resin column), No. 19 column (styrenic anion resin column) and No. 20 column (acrylic anion resin column), in which No. 18 column (acrylic anion resin column) and No. 20 column (acrylic anion resin column) were connected in series, and the regeneration solution flowed through No. 18 column and No. 20 column in sequence.
The rinsing section comprised a plurality of resin columns, in which the acrylic anion resin columns and the styrenic anion resin columns were arranged alternatively, and the same kind of resin columns were connected in series, as shown in Figure 3, the rinsing section comprised No. 14 column (acrylic anion resin column), No. 15 column (styrenic anion resin column) and No. 16 column (acrylic anion resin column), in which the No. 14 column and No. 16 column were connected in series, and water flowed through the No. 14 column and No. 16 column in sequence. 10 IEC232028PCT
At the same time, No. 16 column was connected in series with No. 18 column in the regeneration section, and the No. 16 and No. 18 columns were of the same kind. After switching, as shown hr 505449
Figure 4, the rinsing section comprised No. 15 column (styrenic anion resin column), No. 16 column (acrylic anion resin column) and No. 17 column (styrenic anion resin column), in which the No. 17 column (styrenic anion resin column) and No. 19 column (styrenic anion resin column) in the regeneration section were connected in series.
Example 3, The system of Example 2 was used to decolorize sucrose (the amount of resin was based on the level of the small test, and there were also 20 columns, 10 columns of each kind).
The decolorization section was divided into first-stage decolorization (even-numbered columns filled with acrylic anion resin) and second-stage decolorization (odd-numbered columns filled with styrenic anion resin), as shown in Figure 1, a sucrose solution was introduced into the columns for decolorization in a countercurrent manner (bottom in, top out), feed conditions: 6L/h, 70°C, Bx 55%, pH 8.51, chromatic value 1165 ICUMSA, fed into the resin columns in the direction of the arrow shown in the diagram, and the feed volume was 30L. The discharge was collected for the determination of pH and chromatic value. The adsorption resins used in the resin column were shown in Table 1. Figure 3 shows the arrangement of the resin columns in cycle one. When the No. 4 column shown in Figure 3 was saturated, it was switched to the next cycle, that was, the arrangement of the resin columns shown in Figure 4. The following shows the material entry in other sections as shown in Figure 4.
In the sweet off section, as shown in Figure 4, 400ml of pure water was introduced into the top of No. 2 column, as shown in Figure 4, which was connected series with No. 3 and No. 4 columns, and the water was discharged from the bottom of No. 4 column. After several cycles of switching, the No. 4 column would be transferred to the backwashing section, regeneration section and rinsing section in turn.
In the backwashing section, water was introduced into the bottom of No. 1 column shown in
Figure 4, and the water was discharged from the top of No. 1 column to backwash the resin.
In the regeneration section, columns arranged in series were used for regeneration. Because the resin columns were filled with two different kinds of resins alternatively, the columns arranged in series for regeneration were two adjacent odd-numbered columns arranged in series as a group for regeneration; two adjacent even-numbered columns arranged in series were used as another group for regeneration; only one group was regenerated in each cycle, and the two groups were regenerated alternately in turn. As shown in Figure 4, 400ml of regeneration agent 11 IEC232028PCT that was a mixed solution of NaCl with a concentration of 10% and NaOH with a concentration
LU505449 of 0.5% was introduced into the top of No. 18 column, discharged from the bottom of No. 18 column, then introduced into No.20 column, and discharged from the bottom of No.20 column, in which the first 160ml was discharged to a wastewater neutralization tank, and then the last 240ml was discharged to a brine recovery tank.
The rinsing section comprised: (1) Slow rinsing, 400ml of pure water was introduced into the top of No. 15 column, and the water was discharged from the bottom, then introduced into
No. 17 and No. 19 columns in turn, and discharged from the bottom of No. 19 column, in which the first 200ml was discharged to the brine recovery tank, and then the last 400ml was discharged to the wastewater neutralization tank; (2) Fast rinsing, pure water was introduced into the top of the No. 15 column to elute the residual sodium chloride and sodium hydroxide in the column, and discharged from the bottom to the wastewater neutralization tank.
The above system for decolorization of sucrose solution was repeatedly regenerated 20 times (20 cycles), and the pH values and chromatic values of the sucrose solutions discharged in the 1% 5% 10% 15% and 20" cycles were detected, the detection data are shown in Table 2; and the exchange performance analysis data of the resins after 20 cycles are shown in Table 3.
Table 1: Resins used in Example 3
Number of resin Resin volume of single
Kind of resin Ion form column column (ml)
Styrenic strong
Odd-number column OH 400 base anion resin
Example 3 _
Even-numbered Acrylic strong ) OH 400 column base anion resin
Table 2: Parameters of sucrose solution discharged in each cycle of Example 3
J
Table 3: Resin exchange performance parameters after 20 cycles in Example 3
Total exchange capacity (equivalent/L resin)
Resin column No. Reduction rate (%) 12 IEC232028PCT
Oddrmumbered column | 1.108 05449
Comparative Example 1
The resins packed in the odd- and even-numbered resin columns were all styrenic strong base anion resin, and the decolorization and purification of the sucrose solution were carried out in the same way as in Example 3. The resin used in this comparative example was shown in
Table 4 below.
The sweet off, backwashing, regeneration, and rinsing processes of the decolorization system were the same as in Example 3.
The above system for decolorization of sucrose solution was repeatedly regenerated 20 times (20 cycles), and the pH values and chromatic values of the sucrose solutions discharged in the 1% 5% 10% 15% and 20" cycles were detected as in Example 3, and the detection data are shown in Table 5; and the analytical data of the exchange resin after 20 cycles are shown in
Table 6.
Table 4: Resin used in Comparative Example 1
Resin volume of
Resin column number Kind of resin Ion form | … single column (ml)
Comparative | Odd- and even-numbered | Styrenic strong
OH 400
Example 1 columns base anion resin
Table 5: Parameters of sucrose solution discharged in each cycle of Comparative Example 1
Table 6: Resin exchange performance parameters after 20 cycles in Comparative Example 1
Total exchange capacity (equivalent/L resin) | Reduction
Number of resin column _ role C9)
Odd- and even-numbered column 1.108
The comparison results between Example 3 and Comparative Example 1 are shown in 13 IEC232028PCT
Figure 7 and Figure 8; after 20 cycles of cyclic decolorization, Comparative Example 1 shows a chromatic value increased by about 56.8% compared with Example 3, indicating a relatively 99 large extent of increase; and Comparative Example 1 also shows a greater reduction of pH value compared with Example 3. The changes of pH value and chromatic value of Example 3 are more stable.
According to the results in Table 3 and Table 6, it could be seen that the acrylic anion exchange resin in the even-numbered column as the first-stage decolorization column can effectively adsorb macromolecular pigments and is not easily polluted by pigments and the like, so that the rapid fouling of the styrenic anion resin in the odd-numbered columns as the second-stage decolorization column can be avoided. Compared with Comparative Example 1,
Example 3 can effectively suppress the reduction of the total exchange capacity of the styrenic anion resin, and the reduction extent of resin exchange capacity in Comparative Example 1 is about 11.8% higher than that of Example 3.
Comparative Example 2 (small test level)
Floating bed ion-exchange two-stage decolorization method was adopted, which consisted of 4 columns, one for use and one for backup; 1# column was filled with acrylic strong base anion resin, 2# column was filled with styrenic strong base anion resin, 1# column and 2# column were connected in series for passing material to carry out two-stage decolorization; 3# column and 4# column were the same as 1# and 2# columns, respectively, which were used as regeneration and backup columns. The specific process is shown in Figures 5 and 6.
Decolorization: The feeding method for decolorization was the same as that in Example 3, except that there were only two floating beds with larger volume. The material entered countercurrently from the bottom of 1# column, passed through the resin layer and was discharged from the top, then was introduced into the bottom of 2# column, and was discharged from the top after being adsorbed by the resin layer;
After 1# and 2# resin columns were saturated by adsorption, they were transferred to the sweet off process, backwashing process, regeneration process, and rinsing process. At the same time, 3# column and 4# column entered the decolorization process until 3# column and 4# column were also saturated by adsorption. This was one cycle.
In Example 3, a plurality of columns performed different processes at the same time. In
Comparative Example 2, only one group of columns performed decolorization, and the other group of columns performed other processes in sequence. 14 IEC232028PCT
The resin used in this comparative example is shown in Table 7, and one cycle of the decolorization system of this comparative example was divided into 5 time periods equally, and 505449 the pH values and chromatic values of the discharged sucrose solution in different time periods were detected, and the average values of repeated 3 cycles were taken, the data of the discharges of these 5 time periods could correspond to the pH values and the chromatic values of the discharged sucrose solutions in the 1%, 5% 10% 15% 20% cycle of Example 3 (for the convenience of corresponding to Example 3, the cycles were directly written as cycle 1, 5, 10, 15, and 20), and the detection data are shown in Table 7, Table 8, and Figures 9 and 10.
Table 7: Resins used in Comparative Example 2
Number of resin Resin volume of single
Ta | eee een ms wm
Comparative base anion resin
Example 2 Styrenic strong 2# column OH 4000
Table 8: Parameters of sucrose solution discharged in each cycle of Comparative Example 2
According to the comparison between Table 7, Table 8 and Tables 1 and 2, as well as the curves in Figures 9 and 10, it could be seen that the detection indexes of discharges in cycles of
Comparative Example 2 change significantly in larger extent than those of Example 3, and the pH and chromatic values are not as stable as Example 3. The greater changes in the detection indexes of the discharges will significantly impact on the quality. The quality of the discharged material of Comparative Example 2 is lower than that of Example 3.
According to the comparison of the resin amounts of the two, the resin amount of Example 3 is reduced by 50%; at the same time, because Example 3 adopts small column, the influents in the columns of the sweet off, rinsing, backwash, regeneration processes have a small pressure, are uniformly distributed in the columns, and thus the regeneration agent and water can be effectively saved. 15 IEC232028PCT
The above description of the disclosed examples is provided to enable any person skilled in
LU505449 the art to make or use the present invention. Various modifications to these examples will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other examples without departing from the spirit or scope of the present invention. Therefore, the present invention will not be limited to the examples shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. 16 IEC232028PCT
Claims (4)
1. A method for sucrose decolorization, comprises the following processes: (1) Decolorization process: after feeding a sucrose solution into a plurality of acrylic anion resin columns arranged in parallel, feeding an effluent thereof into a plurality of styrenic anion resin columns arranged in parallel, thereby performing two-stage decolorization, in which the sucrose solution in the decolorization process has a temperature of 70 to 80 °C, and a sucrose mass percentage concentration of 50 to 55%; (2) Sweet off process: by using water carrying out sweet off process in an acrylic anion resin column and a styrenic anion resin column switched from the decolorization process; (3) Backwashing process: by using water backwashing an acrylic anion resin column and a styrenic anion resin column switched from the sweet off process; (4) Regeneration process: by using a regeneration solution regenerating an acrylic anion resin column and a styrenic anion resin column switched from the backwashing process, wherein the regeneration solution is a mixed solution of a NaCl solution with a mass percentage concentration of 8 to 10% and a NaOH solution with a mass percentage concentration of 0.5 to
1.0%; (5) Rinsing process: by using water rinsing an acrylic anion resin column and a styrenic anion resin column switched from the regeneration process; Wherein, the acrylic anion resin columns and the styrenic anion resin columns in the decolorization process, sweet off process, backwashing process, regeneration process, and rinsing process are switched in sequence; The acrylic anion resin columns and the styrenic anion resin columns in the decolorization process, sweet off process, backwashing process, regeneration process and rinsing process are arranged alternatively, and switched according to the order of the process positions where the resin columns are located when switching, and only one resin column is switched each time; The same kind of resin columns are arranged and treated in series during the rising process and the regeneration process.
2. The method for sucrose decolorization according to claim 1, wherein in the regeneration process, during one switching cycle, the regeneration solution only regenerates one kind of resin column, and during the next switching cycle, another kind of resin column is regenerated. 17 IEC232028PCT
3. A system for sucrose decolorization, comprising:
Decolorization section: comprising an acrylic anion resin column unit and a styrenic anion resin column unit, in which the acrylic anion resin column unit and the styrenic anion resin column unit are connected in series, the acrylic anion resin column unit comprises a plurality of acrylic anion resin columns connected in parallel, the styrenic anion resin column unit comprises a plurality of styrenic anion resin columns connected in parallel, the decolorization section has an influent of sucrose solution, the sucrose solution has a temperature of 70 to 80°C and a sucrose mass percentage concentration of 50 to 55%;
Sweet off section: comprising an acrylic anion resin column and a styrenic anion resin column switched from the decolorization section, in which the sweet off section has an influent of water;
Backwashing section: comprising an acrylic anion resin column and a styrenic anion resin column switched from the sweet off section, in which the backwashing section has an influent of water;
Regeneration section: comprising an acrylic anion resin column and a styrenic anion resin column switched from the backwashing section, in which a regeneration solution is a mixed solution of a NaCl solution with a mass percentage concentration of 8 to 10% and a NaOH solution with a mass percentage concentration of 0.5 to 1.0%;
Rinsing section: comprising an acrylic anion resin column and a styrenic anion resin column switched from the regeneration section, in which the rinsing section has an influent of water;
Wherein, the acrylic anion resin columns and the styrenic anion resin columns in the decolorization section, sweet off section, backwashing section, regeneration section, and rinsing section are switched according to the sequence of processes;
The acrylic anion resin columns and the styrenic anion resin columns in the decolorization section, sweet off section, backwashing section, regeneration section and rinsing section are arranged alternatively, and switched according to the order of the process positions where the resin columns are located when switching, and only one resin column is switched each time;
The same kind of resin columns are arranged and treated in series in the rinsing section and the regeneration section.
18 IEC232028PCT
4. The system for sucrose decolorization according to claim 3, wherein, in one switching cycle, only one kind of resin column in the regeneration section is communicated with a 509449 regeneration solution inlet pipe, and in the next switching cycle, another kind of resin column in the regeneration section is communicated with a regeneration solution inlet pipe, and at the same time, the last resin column in the rinsing section is communicated in series with the same kind of resin column in the regeneration section. 19 IEC232028PCT
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210240595.2A CN114606348A (en) | 2022-03-10 | 2022-03-10 | Sucrose decoloring method and system |
| CN202210745626.XA CN114807456B (en) | 2022-03-10 | 2022-06-29 | Sucrose decoloring method and system |
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| LU505449A1 true LU505449A1 (en) | 2023-12-11 |
| LU505449B1 LU505449B1 (en) | 2024-03-11 |
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| CN (2) | CN114606348A (en) |
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| WO (1) | WO2023169166A1 (en) |
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| CN114606348A (en) * | 2022-03-10 | 2022-06-10 | 欧尚元(天津)有限公司 | Sucrose decoloring method and system |
| CN117583038B (en) * | 2024-01-18 | 2024-04-12 | 欧尚元智能装备有限公司 | Sucrose decalcification method and system |
| CN117599860B (en) * | 2024-01-23 | 2024-03-26 | 欧尚元智能装备有限公司 | Cephalosporium decoloring system and process |
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| CN100401916C (en) * | 2006-03-15 | 2008-07-16 | 浙江大学 | Decoloring method for heliangine lixiviation liquid |
| CN102031315B (en) * | 2010-11-30 | 2013-08-07 | 华南理工大学 | Method for regenerating sugar making decolorized and decalcified resin and method for recycling regeneration waste liquid |
| JP6283235B2 (en) * | 2014-02-25 | 2018-02-21 | オルガノ株式会社 | Method and apparatus for purifying sucrose solution |
| CN109225355B (en) * | 2018-11-13 | 2023-11-14 | 赛普特环保技术(厦门)有限公司 | Continuous ion exchange process for removing inorganic salt and system adopted by same |
| CN209138051U (en) * | 2018-11-13 | 2019-07-23 | 赛普特环保技术(厦门)有限公司 | A kind of mobile resin column system for xylose removal of impurities |
| CN111254230B (en) * | 2020-03-04 | 2022-04-12 | 德兰梅勒（北京）分离技术股份有限公司 | Refined sugar decoloring device and decoloring, backwashing, regenerating and cleaning processes |
| CN112062796B (en) * | 2020-10-30 | 2022-02-22 | 石药集团圣雪葡萄糖有限责任公司 | Acarbose continuous desalting and neutralizing production method based on continuous ion exchange device |
| CN112619713A (en) * | 2020-12-30 | 2021-04-09 | 保龄宝生物股份有限公司 | Ion exchange system for producing functional oligosaccharide and use method thereof |
| CN114606348A (en) * | 2022-03-10 | 2022-06-10 | 欧尚元(天津)有限公司 | Sucrose decoloring method and system |
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| CN114807456A (en) | 2022-07-29 |
| WO2023169166A1 (en) | 2023-09-14 |
| CN114807456B (en) | 2023-01-13 |
| LU505449B1 (en) | 2024-03-11 |
| CN114606348A (en) | 2022-06-10 |
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