CN117225483B - Combined valve array multi-unit continuous ion exchange system - Google Patents
Combined valve array multi-unit continuous ion exchange system Download PDFInfo
- Publication number
- CN117225483B CN117225483B CN202311501100.8A CN202311501100A CN117225483B CN 117225483 B CN117225483 B CN 117225483B CN 202311501100 A CN202311501100 A CN 202311501100A CN 117225483 B CN117225483 B CN 117225483B
- Authority
- CN
- China
- Prior art keywords
- valve
- column
- resin
- valve array
- resin columns
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000005342 ion exchange Methods 0.000 title claims abstract description 37
- 239000011347 resin Substances 0.000 claims abstract description 252
- 229920005989 resin Polymers 0.000 claims abstract description 252
- 238000011069 regeneration method Methods 0.000 claims abstract description 75
- 230000008929 regeneration Effects 0.000 claims abstract description 73
- 238000004519 manufacturing process Methods 0.000 claims abstract description 49
- 238000002386 leaching Methods 0.000 claims abstract description 41
- 238000011001 backwashing Methods 0.000 claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 238000000034 method Methods 0.000 claims abstract description 27
- 239000000463 material Substances 0.000 claims abstract description 25
- 230000003068 static effect Effects 0.000 claims abstract description 18
- 238000002791 soaking Methods 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 50
- 238000007670 refining Methods 0.000 claims description 39
- 239000002253 acid Substances 0.000 claims description 5
- 235000009508 confectionery Nutrition 0.000 claims description 5
- 239000011159 matrix material Substances 0.000 claims description 5
- 239000003513 alkali Substances 0.000 claims description 4
- 238000009825 accumulation Methods 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 2
- 230000002787 reinforcement Effects 0.000 abstract description 8
- 230000002035 prolonged effect Effects 0.000 abstract description 7
- 238000003491 array Methods 0.000 description 24
- 238000007599 discharging Methods 0.000 description 9
- 238000005728 strengthening Methods 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- 150000002500 ions Chemical class 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 238000006386 neutralization reaction Methods 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 230000001172 regenerating effect Effects 0.000 description 3
- 150000001450 anions Chemical class 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 2
- 230000003014 reinforcing effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- OWEGMIWEEQEYGQ-UHFFFAOYSA-N 100676-05-9 Natural products OC1C(O)C(O)C(CO)OC1OCC1C(O)C(O)C(O)C(OC2C(OC(O)C(O)C2O)CO)O1 OWEGMIWEEQEYGQ-UHFFFAOYSA-N 0.000 description 1
- 229920001353 Dextrin Polymers 0.000 description 1
- 239000004375 Dextrin Substances 0.000 description 1
- 229930091371 Fructose Natural products 0.000 description 1
- RFSUNEUAIZKAJO-ARQDHWQXSA-N Fructose Chemical compound OC[C@H]1O[C@](O)(CO)[C@@H](O)[C@@H]1O RFSUNEUAIZKAJO-ARQDHWQXSA-N 0.000 description 1
- 239000005715 Fructose Substances 0.000 description 1
- GUBGYTABKSRVRQ-PICCSMPSSA-N Maltose Natural products O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@@H]1O[C@@H]1[C@@H](CO)OC(O)[C@H](O)[C@H]1O GUBGYTABKSRVRQ-PICCSMPSSA-N 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- GUBGYTABKSRVRQ-QUYVBRFLSA-N beta-maltose Chemical compound OC[C@H]1O[C@H](O[C@H]2[C@H](O)[C@@H](O)[C@H](O)O[C@@H]2CO)[C@H](O)[C@@H](O)[C@@H]1O GUBGYTABKSRVRQ-QUYVBRFLSA-N 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 235000019425 dextrin Nutrition 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 230000009191 jumping Effects 0.000 description 1
- 235000014655 lactic acid Nutrition 0.000 description 1
- 239000004310 lactic acid Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention discloses a combined valve array multi-unit continuous ion exchange system, wherein a plurality of positive resin columns and a plurality of negative resin columns are alternately arranged in sequence from left to right on a process position, and flow rates of a feeding flowmeter, a backwashing flow meter, a leaching flow meter, a regeneration liquid A and a regeneration liquid B flow meter and the like are respectively controlled by self-control valves to realize sequential circulation switching of each period, so that the materials are subjected to ion exchange treatment, and meanwhile, the circulating static soaking of all the positive resin columns and the negative resin columns is realized in one large period to recover the exchange capacity of resin. According to the invention, the positive resin columns and the negative resin columns are alternately regenerated in different periods, so that the use quantity of the resin columns is reduced, and the production input cost is reduced; and a static valve array is added into the whole system, and each cycle carries out reinforcement regeneration on one resin column, and after one large cycle, the resin columns in the whole system are all subjected to reinforcement regeneration, so that the service life of the resin columns is prolonged.
Description
Technical Field
The invention relates to the technical field of ion exchange, in particular to a combined valve array multi-unit continuous ion exchange system.
Background
Ion exchange is a unit operation belonging to mass transfer separation process by means of ion exchange between ions in ion exchange resin exchanger and ions in dilute solution to achieve the goal of extracting or removing some ions in solution. Ion exchange is a reversible equivalent exchange reaction. At present, the resin is widely applied to the starch sugar industry and the fermentation industry, and products such as fructose, maltose, dextrin, lactic acid and the like are utilized to remove anions and cations in the products. In a valve array system of continuous ion exchange equipment, the patent number is CN208115777U, the production valve array, the refining valve array, the water ejection valve array, the leaching valve array, the regeneration valve array and the backwashing valve array in the male column valve array and the female column valve array are disclosed, the ratio of the leaching valve array to the regeneration valve array to the backwashing valve array is 5:5:3:3:3:1 respectively, 40 resin columns are used in total, the corresponding self-control valves are more, the complexity is higher, and ion exchange errors are easy to occur in the ion exchange process; meanwhile, the water ejection valve array, the leaching valve array, the regeneration valve array and the backwashing valve array are mainly used for regenerating the resin in the production valve array and the refining valve array, but the production valve array and the refining valve array are recycled all the time, and the regenerated resin is required to be put into production as soon as possible, and the traditional ion exchange column is only subjected to simple regeneration and not subjected to reinforced regeneration, so that the resin elution efficiency in the resin column does not reach 100 percent, the service life of the resin in industrial production is shorter than that of the resin subjected to reinforced regeneration, the replacement frequency of the resin is increased, the cost input of the resin and the labor input during resin replacement are increased, and the production cost is greatly increased.
Disclosure of Invention
In view of the above-mentioned drawbacks or shortcomings of the prior art, an object of the present invention is to provide a combined multi-unit valve array, so as to reduce the number of resin columns used and reduce the complexity of the whole valve array; meanwhile, a circulating static valve array is arranged in the valve array, so that each resin column is subjected to static soaking in different periods, the reinforced regeneration of the resin is realized, and the service life of the resin is prolonged.
According to the technical scheme provided by the embodiment of the application, in the combined valve array multi-unit continuous ion exchange system, a plurality of positive resin columns and a plurality of negative resin columns are alternately arranged in sequence from left to right on a process position, the process position formed by the plurality of positive resin columns and the plurality of negative resin columns comprises a water top sugar valve array, a positive column production valve array, a negative column production valve array, a positive column refining valve array, a negative column refining valve array, a leaching valve array, a regeneration valve array, a static valve array and a backwashing valve array, wherein the number ratio of columns of each valve array is 3:5:5:5:5:4:3:1:1, a step of; each positive resin column and each negative resin column are provided with self-control valves, and the sequential circulation switching of each period is realized by controlling the flow rates of a feeding flowmeter, a backwashing inflow flowmeter, a leaching inflow flowmeter, a regenerated liquid A and a regenerated liquid B flowmeter and the like, so that the material is subjected to ion exchange treatment, and meanwhile, the circulating static soaking of all the positive resin columns and the negative resin columns is realized in one large period so as to recover the exchange capacity of the resin;
The system is characterized in that the male column production valve array is formed by connecting a plurality of groups of male resin columns in parallel, the female column production valve array is formed by connecting a plurality of groups of female resin columns in parallel, the male column production valve array and the female column production valve array are alternately arranged, the male column refining valve array is formed by connecting a plurality of groups of male resin columns in parallel, the female column refining valve array is formed by connecting a plurality of groups of female resin columns in parallel, the male column refining valve array and the female column refining valve array are alternately arranged, and regeneration and leaching of one resin column are realized in each period.
Preferably, the water top sugar valve array is formed by connecting a plurality of groups of positive resin columns and negative resin columns in series, so that the water top sugar valve array can directly act on the positive resin columns and the negative resin columns.
Preferably, the leaching valve array and the regeneration valve array are formed by connecting a plurality of resin columns in series end to end.
Preferably, the plurality of positive resin columns and the plurality of negative resin columns adopt a PLC control system, and the period and the switching of the resin columns are realized by controlling the flow rate and the accumulation volume of the flowmeter.
Preferably, the regeneration liquid A and the regeneration liquid B are acid liquid and alkali liquid respectively, and when the resin columns with different properties are regenerated, different regeneration liquids are introduced, so that the reduction of the number of the resin columns is realized.
Preferably, 14 self-control valves are arranged on each positive resin column and each negative resin column, and each self-control valve comprises a regeneration liquid inlet valve, a salt inlet valve, a water top sugar inlet valve, a leaching inlet valve, a backwashing outlet valve, a production inlet valve and a refining inlet valve; the device comprises a string column valve, a jump column valve, a sweet water valve, a blow-down valve, a production valve, a refined outlet valve and a backwashing inlet valve, and the periodic switching of the resin column is realized through the opening and closing of the valve.
In summary, the application has the following beneficial effects: the application has the following advantages:
1. according to the invention, the water top sugar valve array is connected in series through the positive resin column and the negative resin column, so that the effect on the positive resin column and the negative resin column can be realized, and the number of resin columns in the traditional water top sugar valve array is reduced;
2. The system uses 32 resin columns in total, compared with 40 resin columns used in the traditional female column valve array and male column valve array, the total number of the resin columns is saved, the purchasing cost is reduced, and meanwhile, the use complexity is reduced;
3. According to the invention, the resin columns in different periods are sequentially and circularly switched, so that the regeneration valve array can be switched into the female column regeneration valve array and the male column regeneration valve array, different types of resin columns are eluted in different periods, and the female column regeneration valve array and the male column regeneration valve array are not required to be arranged at the same time like the traditional valve array, so that the use quantity of the regeneration valve array is reduced; the same backwashing valve array and the leaching valve array are sequentially and circularly switched along with different periods, and different resin column types are subjected to resin cleaning in different periods, so that the total number of the resin columns and the complexity of the valve array are further reduced;
4. According to the invention, the static valve array is arranged in the valve array, and when the valve array is sequentially and circularly switched in a large period, all the resin columns can be sequentially and statically soaked and regenerated in a circulating way, so that the reinforced regeneration of the resin columns is realized, the service life of the resin columns is prolonged, the replacement frequency of the resin in the resin columns is reduced, the input cost of the resin and the labor cost in the resin replacement process are reduced, namely the production cost in the production process is reduced, and the production profit is improved.
Drawings
Other features, objects and advantages of the present application will become more apparent upon reading of the detailed description of non-limiting embodiments, made with reference to the accompanying drawings in which:
FIG. 1 is a schematic illustration of a resin column of the present invention, designated 25, in a stationary valve array;
FIG. 2 is a schematic illustration of a resin column of the present invention, designated 26, in a stationary valve array;
FIG. 3 is a schematic representation of the resin column of the present invention, designated 27, in a stationary valve array.
Reference numerals 1'-32' are process positions, and reference numerals 1-32 are resin column numbers.
Detailed Description
The application is described in further detail below with reference to the drawings and examples. It is to be understood that the specific embodiments described herein are merely illustrative of the application and are not limiting of the application. It should be noted that, for convenience of description, only the portions related to the application are shown in the drawings.
It should be noted that, without conflict, the embodiments of the present application and features of the embodiments may be combined with each other. The application will be described in detail below with reference to the drawings in connection with embodiments.
Example 1
As shown in fig. 1, the 32 resin columns are sequentially arranged from left to right, and the rectangular frames vertically placed are resin columns, and the marks in the frames above the resin columns are as follows: 1.2, 3, 4 … are the labels of the resin column, the label in the square frame below the resin column, such as 1 ,、2,、3,、4,、5,…32, is the label of the process position, the process position comprises a water top sugar valve array, a male column production valve array, a female column production valve array, a male column refining valve array, a female column refining valve array, a leaching valve array, a regeneration valve array, a static valve array and a backwashing valve array, namely the process position is always from left to right, the No.1 resin column in the rectangular frame is filled with positive resin, and the No. 2 resin column in the square frame is filled with negative resin, so that the left-right positive resin column and the negative resin column are alternately arranged;
three resin columns which are positioned at the leftmost side and connected in series are a water top sugar valve array, and the resin columns are numbered 1, 2 and 3;
five parallel female column production valve arrays are sequentially arranged right, and resin columns with the numbers of 4, 6, 8, 10 and 12 are arranged right; and five parallel connected male column production valve arrays, namely, resin columns with the numbers of 5, 7, 9, 11 and 13 are connected in parallel at intervals;
Five parallel female column refining valve arrays are sequentially arranged right, and resin columns with the reference numbers of 14, 16, 18, 20 and 22 are arranged right; and five parallel-connected male column refining valve arrays, namely resin columns with the numbers of 15, 17, 19, 21 and 23, namely one resin column is arranged in parallel at intervals;
Four resin columns of the same type which are connected in series are sequentially arranged right to form a leaching valve array, and the resin columns are numbered 24, 26, 28 and 30; 1 static valve array is arranged in the gap of the leaching valve array, and the resin column is marked with the reference number 25; and three regeneration valve arrays, namely resin columns 27, 29 and 31, which are connected in series;
The rightmost end is provided with 1 backwashing valve array and a resin column with the reference numeral 32.
When in use, as shown in figure 1, raw materials to be purified enter 5 parallel male column production valve arrays from a material inlet pipe, then enter 5 parallel female column production valve arrays through a pipeline, enter 5 parallel male column refining valve arrays through a transfer pump and a pipeline after exiting the female column production valve arrays, then enter 5 parallel female column refining valve arrays after discharging, and enter the next procedure after discharging.
When the resin column processes a certain volume of material, i.e. a set accumulated volume is reached, the sequential switching is carried out, specifically, one resin column is sequentially switched in each period, for example, the No. 26 resin column in the figure 1 is switched to a static valve array, the No. 26 resin column is subjected to the strengthening regeneration, the rest resin columns are sequentially switched to the figure 2 in the figure 1,
Three resin columns which are connected in series and are arranged in sequence from the leftmost end are a water top sugar valve array, and the resin columns are numbered 2, 3 and 4;
Five parallel male column production valve arrays are sequentially arranged right, and resin columns with the numbers of 5, 7, 9, 11 and 13 are arranged right; and five parallel female column production valve arrays, namely resin columns with the numbers of 6, 8, 10, 12 and 14 are connected in parallel at intervals;
Five parallel male column refining valve arrays are sequentially arranged rightward, and resin columns with the numbers of 15, 17, 19, 21 and 23 are arranged; and five parallel female column refining valve arrays, namely, resin columns with the reference numbers of 16, 18, 20, 22 and 24 are connected in parallel at intervals;
four resin columns of the same type which are connected in series are sequentially arranged right to form a leaching valve array, and the resin columns are numbered 25, 27, 29 and 31; setting 1 static valve array to the right in the clearance of the leaching valve array, and the resin column with the reference number of 26; and three series connected regeneration valve arrays, resin columns 28, 30, 32;
continuously feeding into five parallel male column production valve arrays, female column production valve arrays, male column refining valve arrays and female column refining valve arrays through a feeding pipe;
Meanwhile, the No. 26 resin column is not fed, namely, the No. 26 resin column is subjected to reinforcement regeneration.
The method comprises the following specific steps:
A. Water top sugar procedure: the condensed water is led into a resin column in a water top sugar valve array with the number of 2, and is output through a resin column in a water top sugar valve array with the number of 4, and is conveyed to a feed front tank with high concentration and a sweet water tank with low concentration;
B. backwashing: introducing condensed water or quick leaching reuse water into a resin column of a backwashing valve array with the number 1, automatically backwashing the resin column with the number 1 through a set program, and finally outputting the resin column into an ion exchange wastewater storage tank;
C. Regeneration procedure: introducing the regenerated liquid B (alkaline solution) through a resin column in a regeneration valve array with the reference number 28, outputting the regenerated liquid B from the resin column in the regeneration valve array with the reference number 32, regenerating the resin column, and delivering regenerated waste liquid to a sewage neutralization tank;
In the regeneration process, when the No. 26 resin column is regenerated by using the regeneration liquid B, the resin column is soaked, so that the reinforcing regeneration of the No. 26 resin column is realized.
D. Slow wash procedure: when the female resin column is regenerated, the male resin column is simultaneously slowly rinsed. Introducing condensed water to a resin column in a leaching valve array with the reference number of 25, then outputting the condensed water by the resin column in the leaching valve array with the reference number of 31, slowly leaching the resin column, eluting acid and redundant ions in the resin column, and delivering the eluted solution to a sewage neutralization tank;
E. A fast leaching state: and (3) introducing condensed water to a resin column in a leaching valve array with the reference number of 25, then conveying discharged water into a backwashing column with the reference number of 1 through a backwashing inlet pipeline, and discharging the backwashed water to an ion exchange wastewater storage tank. The purpose is to clean the free acid in the No. 25 resin column with a large flow of water. And the waste water discharged from leaching is reused to backwash the backwash column with the backwash mark 1, so that water is saved.
Therefore, the No. 26 resin column in FIG. 1 is switched from the leaching valve array to the static valve array shown in FIG. 2, namely, the process position No. 25' is switched to be one period, and after the conversion, the processes of producing the valve array, refining the valve array, strengthening regeneration, leaching and the like are simultaneously carried out, so that the regeneration time of the resin column is greatly saved, the strengthening regeneration of the resin in the resin column can be realized, and the service life of the resin is prolonged.
Example 2
As shown in fig. 2, the 32 resin columns are sequentially arranged from left to right, and the rectangular frames vertically placed are resin columns, and the marks in the frames above the resin columns are as follows: 1. 2, 3, 4 … are the labels of the resin column, the label in the square frame below the resin column, such as 1 ,、2,、3,、4,、5,…32, is the label of the process position, the process position comprises a water top sugar valve array, a male column production valve array, a female column production valve array, a male column refining valve array, a female column refining valve array, a leaching valve array, a regeneration valve array, a static valve array and a backwashing valve array, namely the process position is always from left to right, the No. 1 resin column in the rectangular frame is filled with positive resin, and the No. 2 resin column in the square frame is filled with negative resin;
As shown in fig. 3, after a certain volume of material is processed by the resin column, i.e. after reaching a set accumulation volume, sequentially switching, specifically, switching one resin column in each period in sequence, for example, switching the number 27 resin column in fig. 2 into a static valve array, performing reinforcement regeneration on the number 27 resin column at this time, and switching the rest resin columns from fig. 2 into fig. 3 in sequence;
three resin columns which are connected in series and are arranged in sequence from the leftmost end are a water top sugar valve array, and the resin columns are numbered 3, 4 and 5;
Five parallel male column production valve arrays, namely 7, 9, 11, 13 and 15 resin columns, are sequentially arranged right; and five parallel female column production valve arrays, namely resin columns with the numbers of 6, 8, 10, 12 and 14 are connected in parallel at intervals;
Five parallel male column refining valve arrays are sequentially arranged rightward, and resin columns with the numbers of 17, 19, 21, 23 and 25 are arranged; and five parallel female column refining valve arrays, namely, resin columns with the reference numbers of 16, 18, 20, 22 and 24 are connected in parallel at intervals;
Four resin columns of the same type which are connected in series are sequentially arranged right to form a leaching valve array, and the resin columns are numbered 26, 28, 30 and 32; 1 static valve array, a resin column with the reference number of 27 and three regeneration valve arrays connected in series, and the resin columns with the reference numbers of 29, 31 and 1 are arranged right in the gap of the leaching valve array;
The resin column with the number of 2 is a backwashing valve array;
after the resin column with the number 27 is switched to be a static valve array, materials are introduced into the positive production valve array, the negative production valve array, the positive refining valve array and the negative refining valve array for ion exchange, and the resin column with the number 27 is subjected to reinforcement regeneration in the process of ion exchange of the materials.
The specific steps are as follows, as shown in figure 3,
A. Water top sugar procedure: the condensed water is led into a resin column in a water top sugar valve array with the number of 3, and is output through a resin column in a water top sugar valve array with the number of 5, and is conveyed to a feed front tank with high concentration and a sweet water tank with low concentration;
B. Backwashing: introducing condensed water or quick leaching reuse water into a resin column of a backwashing valve array with the number of 2, automatically backwashing the resin column with the number of 2 through a set program, and finally outputting the resin column into an ion exchange wastewater storage tank;
C. regeneration procedure: introducing the regenerated liquid A (acid solution) through a resin column in a regeneration valve array with the reference number 29, outputting the regenerated liquid A from the resin column in the regeneration valve array with the reference number 1, regenerating the resin column, and delivering regenerated waste liquid to a sewage neutralization tank;
in the regeneration process, when the No. 27 resin column is regenerated by using the regeneration liquid A, the No. 27 resin column is soaked, so that the reinforcement regeneration of the No. 27 resin column is realized.
D. slow wash procedure: when the resin column is regenerated, the anion resin column is simultaneously rinsed slowly. Introducing condensed water to a resin column in a leaching valve array with the reference number of 26, then outputting the condensed water by the resin column in the leaching valve array with the reference number of 32, slowly leaching the resin column, eluting alkali and redundant ions in the resin column, and delivering the eluted solution to a sewage neutralization tank;
E. a fast leaching state: and (3) introducing condensed water to a resin column in a leaching valve array with the reference number of 26, then conveying discharged water into a backwashing column with the reference number of 2 through a backwashing inlet pipeline, and discharging the backwashed water to an ion exchange wastewater storage tank. The purpose is to clean the free alkali in the No. 26 resin column with a large flow of water. And the waste water discharged from leaching is reused to backwash the backwash column with the backwash mark 2, so that water is saved.
As can be seen from example 2, during ion exchange of the material, the resin column designated 27 was subjected to enhanced regeneration and rinsing, which is the second cycle of ion exchange treatment of the material and enhanced regeneration of the resin column.
As can be seen from the combination of examples 1 and 2, in the third cycle, the resin column denoted by 28 was switched out for the enhanced regeneration, and the material ion exchange treatment and the enhanced regeneration of the resin column denoted by 28 were also achieved at this time;
And so on, in the fourth period, the resin column is moved leftwards by one step, the process position is unchanged, and the material ion exchange treatment and the reinforced regeneration of the resin column with the reference number of 29 are realized;
In the fifth period, the resin column working in the fourth period continuously moves leftwards by one time to realize material ion exchange treatment and reinforced regeneration of the resin column with the reference number of 30;
……
and so on, in the thirty-second period, the resin column working in the thirty-first period moves leftwards by one, so as to realize material ion exchange treatment and reinforced regeneration of the resin column with the number of 25;
In the thirty-third period, the resin column working in the thirty-second period moves leftwards by one to realize material ion exchange treatment and reinforced regeneration of the resin column with the reference number of 26;
Therefore, in the first cycle to the thirty-second cycle, all 32 resin columns are subjected to strengthening regeneration respectively, which belongs to a large cycle, and in the process of realizing material ion exchange treatment, strengthening regeneration of all the resin columns can be realized, on one hand, the working efficiency can be improved, on the other hand, strengthening of the regeneration capacity of the resin columns is realized, and the service life of resin in the resin columns is prolonged.
Example 3
Influence of different large-period resin columns on material handling capacity
The reinforced regeneration is carried out according to the switching of the resin columns, the material treatment capacity of each large-period production valve array and the refining valve array is a certain multiple of the resin volume, and the material treatment capacity of the production valve array and the refining valve array for discharging is shown in table 1 after five large-period material treatment:
TABLE 1 Inlet and discharge index Condition Table
As can be seen from Table 1, in the first to fifth large cycles, when the resin column numbered 25 is a stationary valve array, the processing rates of the production valve array and the refining valve array slightly decrease, but after five large cycles, the processing rate of the material can reach more than 97%, which means that the reinforcing regeneration capability of the resin in 32 resin columns in each large cycle reaches the maximum, that is, the resin matrix can reach complete regeneration, so that the service life of the resin column can be prolonged, the replacement frequency of the resin in the resin column can be reduced in production, and the cost can be effectively reduced.
Material handling rate = (feed conductivity-discharge conductivity) ×100%/feed conductivity
In practice, different materials are handled, and there are different cumulative volumes.
The feed-in and regeneration feed-in valve is used for feeding in regeneration liquid, the feed-in valve is used for feeding in brine, the water top sugar feed-in valve is used for feeding in water top sugar, the leaching feed-in valve is used for feeding in leaching liquor, the backwashing feed-out valve is used for feeding in backwashing liquor, the production feed-in valve is used for feeding in materials, and the refining feed-in valve is used for feeding in refining liquid; the column-connecting valve is used for connecting resin columns, the column-jumping valve is used for jumping over the resin columns when a certain column fails or needs to be recovered, the sweet water valve is used for water top sugar liquid discharging, the blow-down valve is used for blow-down, the production valve is used for material discharging, the refined liquid discharging valve is used for refined liquid discharging, and the backwashing inlet valve is used for inlet and backwashing liquid.
FCV in fig. 1, 2 and 3 represents a regulator valve, FT represents a flow meter, and PT represents a pressure transmitter.
In the regeneration process of each cycle, one resin column is separated out to be stationary for reinforcement regeneration, and after one large cycle is completed, 32 resin columns are subjected to reinforcement regeneration, so that the service life of the resin columns can be prolonged, and the production cost is reduced on the other hand.
Although 32 resin columns are used in this scheme, only the positive resin column (or the negative resin column) is regenerated in one cycle; in the next period, only the negative resin columns (or the positive resin columns) are regenerated, so that alternate regeneration of the positive resin columns and the negative resin columns is realized, more resin columns are used instead of the traditional simultaneous regeneration of the positive resin columns and the negative resin columns, the regeneration effect is not influenced, the use amount of the resin columns is saved, the investment of factories to the resin columns is reduced, and the use complexity of a resin ion exchange system is also reduced.
The above description is only illustrative of the preferred embodiments of the application and the technical principles employed. Meanwhile, the scope of the application is not limited to the technical scheme formed by the specific combination of the technical features, and other technical schemes formed by any combination of the technical features or the equivalent features thereof without departing from the inventive concept are also covered. Such as the above-mentioned features and the technical features disclosed in the present application (but not limited to) having similar functions are replaced with each other.
Claims (6)
1. A combined valve array multi-unit continuous ion exchange system is characterized in that:
The process position formed by the plurality of positive resin columns and the plurality of negative resin columns comprises a water top sugar valve array, a positive column production valve array, a negative column production valve array, a positive column refining valve array, a negative column refining valve array, a leaching valve array, a regeneration valve array, a static valve array and a backwashing valve array, wherein the number ratio of the columns of each valve array is 3:5:5:5:5:4:3:1:1, a step of;
Each positive resin column and each negative resin column are provided with self-control valves, and the sequential circulation switching of each period is realized by controlling a feeding flowmeter, a backwashing inflow flowmeter, a leaching inflow flowmeter, a regenerated liquid A and a regenerated liquid B flowmeter respectively, so that the materials are subjected to ion exchange treatment, and meanwhile, the circulating static soaking of all the positive resin columns and the negative resin columns is realized in one large period so as to recover the exchange capacity of the resin;
The system is characterized in that the male column production valve array is formed by connecting a plurality of groups of male resin columns in parallel, the female column production valve array is formed by connecting a plurality of groups of female resin columns in parallel, the male column production valve array and the female column production valve array are alternately arranged, the male column refining valve array is formed by connecting a plurality of groups of male resin columns in parallel, the female column refining valve array is formed by connecting a plurality of groups of female resin columns in parallel, the male column refining valve array and the female column refining valve array are alternately arranged, and regeneration and leaching of one resin column are realized in each period.
2. The modular valve matrix multi-unit continuous ion exchange system of claim 1, wherein: the water top sugar valve array is formed by connecting a plurality of groups of positive resin columns and negative resin columns in series.
3. A modular valve array multi-unit continuous ion exchange system according to claim 2, wherein: the leaching valve array and the regeneration valve array are formed by connecting a plurality of resin columns in series end to end.
4. A modular valve matrix multi-unit continuous ion exchange system according to claim 3, wherein: the positive resin columns and the negative resin columns adopt a PLC control system, and the period and the resin columns are switched by controlling the flow and the accumulation volume of the flowmeter.
5. The modular valve matrix multi-unit continuous ion exchange system of claim 4, wherein: the regenerated liquid A and the regenerated liquid B are acid liquid and alkali liquid respectively.
6. The modular valve matrix multi-unit continuous ion exchange system of claim 5, wherein: each positive resin column and each negative resin column are provided with 14 self-control valves, including a regeneration liquid inlet valve, a salt inlet valve, a water top sugar inlet valve, a leaching inlet valve, a backwashing outlet valve, a production inlet valve and a refining inlet valve; the device comprises a string column valve, a jump column valve, a sweet water valve, a blow-down valve, a production valve, a refined outlet valve and a backwashing inlet valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311501100.8A CN117225483B (en) | 2023-11-13 | 2023-11-13 | Combined valve array multi-unit continuous ion exchange system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311501100.8A CN117225483B (en) | 2023-11-13 | 2023-11-13 | Combined valve array multi-unit continuous ion exchange system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN117225483A CN117225483A (en) | 2023-12-15 |
| CN117225483B true CN117225483B (en) | 2024-05-17 |
Family
ID=89082957
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202311501100.8A Active CN117225483B (en) | 2023-11-13 | 2023-11-13 | Combined valve array multi-unit continuous ion exchange system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN117225483B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3956115A (en) * | 1969-10-11 | 1976-05-11 | Institutul De Proiectari Pentru Industria Chimica Anorganica Si A Ingrasamintelor | Process for the regeneration of ion-exchange resins and applications thereof |
| CN1107808A (en) * | 1994-12-12 | 1995-09-06 | 王廷生 | Regeneration method for double-layer bed in salt removing system for water treatment |
| CN105435865A (en) * | 2015-12-23 | 2016-03-30 | 芜湖美的厨卫电器制造有限公司 | Weak-acid cation-exchange resin regeneration method and application of organic weak acid in regeneration of weak-acid cation-exchange resin |
| CN111450903A (en) * | 2020-05-21 | 2020-07-28 | 浙江华康药业股份有限公司 | Continuous ion exchange system for xylose production and use method thereof |
| CN212732180U (en) * | 2020-05-21 | 2021-03-19 | 浙江华康药业股份有限公司 | Continuous ion exchange system for xylose production |
| CN114699801A (en) * | 2021-09-08 | 2022-07-05 | 欧尚元(天津)有限公司 | Valve array type continuous ion exchange system for purification of red lactic acid |
-
2023
- 2023-11-13 CN CN202311501100.8A patent/CN117225483B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3956115A (en) * | 1969-10-11 | 1976-05-11 | Institutul De Proiectari Pentru Industria Chimica Anorganica Si A Ingrasamintelor | Process for the regeneration of ion-exchange resins and applications thereof |
| CN1107808A (en) * | 1994-12-12 | 1995-09-06 | 王廷生 | Regeneration method for double-layer bed in salt removing system for water treatment |
| CN105435865A (en) * | 2015-12-23 | 2016-03-30 | 芜湖美的厨卫电器制造有限公司 | Weak-acid cation-exchange resin regeneration method and application of organic weak acid in regeneration of weak-acid cation-exchange resin |
| CN111450903A (en) * | 2020-05-21 | 2020-07-28 | 浙江华康药业股份有限公司 | Continuous ion exchange system for xylose production and use method thereof |
| CN212732180U (en) * | 2020-05-21 | 2021-03-19 | 浙江华康药业股份有限公司 | Continuous ion exchange system for xylose production |
| CN114699801A (en) * | 2021-09-08 | 2022-07-05 | 欧尚元(天津)有限公司 | Valve array type continuous ion exchange system for purification of red lactic acid |
Non-Patent Citations (1)
| Title |
|---|
| 霍汉镇.现代制糖工业技术 第1分册.北京：中国轻工业出版社,1992,第87页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN117225483A (en) | 2023-12-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111450903A (en) | Continuous ion exchange system for xylose production and use method thereof | |
| CN212189138U (en) | Valve array type continuous ion exchange system | |
| CN112062796B (en) | Acarbose continuous desalting and neutralizing production method based on continuous ion exchange device | |
| CN106350614B (en) | Comprehensive recycling method for preparing ion exchange water and acid and alkali from maltose syrup | |
| LU505290B1 (en) | Method for purifying L-lactic acid | |
| CN212655517U (en) | Dual-mode switching operation metallurgical wastewater softening device | |
| CN109225355B (en) | Continuous ion exchange process for removing inorganic salt and system adopted by same | |
| CN211913799U (en) | Ion exchange regeneration system | |
| CN117225483B (en) | Combined valve array multi-unit continuous ion exchange system | |
| CN114606349A (en) | Beet syrup softening method | |
| EP0732968A1 (en) | Ion exchange methods and systems incorporating regenerant recycling | |
| CN212732180U (en) | Continuous ion exchange system for xylose production | |
| CN211585316U (en) | System for continuously removing anions in 3-hydroxy-1, 3, 5-pentanedioic acid | |
| CN217628184U (en) | Nucleoside purification system | |
| CN116474419A (en) | Continuous decolorizing system for xylose production and using method thereof | |
| CN212504128U (en) | Ultrafiltration device in reclaimed water recycling system | |
| CS212333B2 (en) | Method of continuous production of dian | |
| CN221085646U (en) | Ion exchange washing system | |
| CN209423642U (en) | A kind of continuous ionic exchange system removing inorganic salts | |
| CN114522743B (en) | Method for preparing sodium iso-vitamin C and decalcification method and system thereof | |
| CN215464472U (en) | Simulated continuous ion exchange production system for glucose syrup | |
| CN214344587U (en) | Separation system of sugar and inorganic salt | |
| CN217016638U (en) | Continuous ion exchange device for purifying phytic acid | |
| CN216172388U (en) | Organic acid continuous ion exchange system | |
| CN117583038B (en) | Sucrose decalcification method and system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |