CN214572048U

CN214572048U - Water-saving and efficient starch sugar ion exchange system

Info

Publication number: CN214572048U
Application number: CN202023175835.0U
Authority: CN
Inventors: 钟雄明; 梁勇
Original assignee: Jiangsu Weituo Automation Technology Co ltd
Current assignee: Jiangsu Weituo Automation Technology Co ltd
Priority date: 2020-12-25
Filing date: 2020-12-25
Publication date: 2021-11-02
Anticipated expiration: 2030-12-25

Abstract

The utility model discloses a water conservation efficient starch sugar ion exchange system, including cation exchange column and anion exchange column, the entry linkage of cation exchange column has into the sugar pipe, first inlet tube and acid inlet pipe, the exit linkage of cation exchange column has first output tube, be connected with first compressed air pipe on the first output tube, the entry linkage of anion exchange column has second inlet tube and alkali inlet pipe, the exit linkage of anion exchange column has the second output tube, be connected with second compressed air pipe on the output tube, still link to each other through drain pipe, sugar discharging pipe between second output tube and the first output tube, first output tube passes through the connecting pipe and links to each other with the entry of anion exchange column, the invention has reduced water consumption, reduction in production cost alleviates environmental protection pressure.

Description

Water-saving and efficient starch sugar ion exchange system

Technical Field

The utility model relates to a starch sugar processing equipment, in particular to starch sugar ion exchange system.

Background

The starch sugar is syrup or powdered sugar product prepared by taking corn starch or rice starch as a raw material and combining an enzyme preparation and other auxiliary materials. Because the starch sugar production has large water consumption and large discharge capacity, some provinces and cities have strict control on starch sugar projects, energy conservation and consumption reduction are required, and the water consumption and discharge capacity are controlled. At present, aiming at traditional high-energy-consumption ion exchange equipment, some manufacturers develop equipment technologies such as floating bed ion exchange and continuous ion exchange to deal with increasingly remarkable environmental protection pressure. Although the floating bed ion exchange has large resin loading and large exchange capacity, compared with the traditional ion exchange, the water-saving capacity is about 30 percent, but the requirement on syrup pretreatment is high, the sugar liquor pretreatment generally adopts ceramic membrane filtration and then enters the ion exchange process, the investment cost is high, and once the resin is polluted, the resin cannot be cleaned in the column; continuous ion exchange is a newer ion exchange process, saves water by about 40 percent compared with the traditional ion exchange, has high requirements on pretreatment of syrup, is complex in valve array formed by valves, influences product quality once the valves leak, and is difficult to investigate.

In the prior art, a few water-saving and efficient schemes about starch sugar ion exchange systems exist, and in a patent 'a water-saving device for cleaning ion exchange resin' (CN 201320599919.9), regenerated waste acid and waste alkali are reused, and in fact, due to the fact that the acid-base concentration is diluted and other impurity ions exist in the waste acid and alkali, the purpose of regeneration cannot be really achieved.

SUMMERY OF THE UTILITY MODEL

The utility model aims at providing a water conservation efficient starch sugar ion exchange system promotes starch sugar production process energy saving and consumption reduction, reduces the manufacturing cost of enterprise, alleviates environmental protection pressure.

The purpose of the utility model is realized like this: the utility model provides a water conservation efficient starch sugar ion exchange system, includes cation exchange column and anion exchange column, the entry linkage of cation exchange column has into sugar pipe, first inlet tube and advances sour pipe, the exit linkage of cation exchange column has first output tube, be connected with first compressed air pipe on the first output tube, the entry linkage of anion exchange column has the second inlet tube and advances alkali pipe, the exit linkage of anion exchange column has the second output tube, be connected with second compressed air pipe on the output tube, still link to each other through drain pipe, sugar discharging pipe between second output tube and the first output tube, first output tube passes through the connecting pipe and links to each other with the entry of anion exchange column.

As a further limitation of the present invention, the outlet of the cation exchange column is provided with a first low liquid level switch, and the outlet of the anion exchange column is provided with a second low liquid level switch.

As a further limitation of the present invention, the first output pipe is further connected with a first backwashing water inlet pipe, and the inlet of the cation exchange column is further connected with a first backwashing water outlet pipe; and the second output pipe is also connected with a second backwashing water inlet pipe, and the inlet of the anion exchange column is also connected with a second backwashing water outlet pipe.

As the utility model discloses a further inject, be connected with mass flow meter on the sugar discharging pipe, be connected with the pH meter on the drain pipe.

Compared with the prior art, the beneficial effects of the utility model reside in that: the utility model can recycle sugar liquor with different concentrations, reduce loss of starch sugar, replace water-topped sugar with syrup in the resin column emptied by the self gravity of the sugar liquor, reduce water consumption, loosen the resin by compressed air, enable the residual syrup and other chemicals in the resin to be more thoroughly cleaned, and simultaneously save water consumption; the mass flow meter, the pH meter and the low liquid level switch are used for respectively monitoring the sugar concentration and the pH of the regenerated water and judging whether the feed liquid is discharged completely, and the regeneration process is controlled more accurately.

Drawings

Fig. 1 is a schematic structural diagram of the present invention.

The device comprises a cation exchange column 1, an anion exchange column 2, a first output end 3, a second output tube 4, a connecting tube 5, a first low liquid level switch 6, a second low liquid level switch 7, a pH meter 8 and a mass flow meter 9.

Detailed Description

As shown in figure 1, a water-saving and high-efficiency starch sugar ion exchange system comprises a cation exchange column 1 and an anion exchange column 2, wherein an inlet of the cation exchange column 1 is connected with a sugar inlet pipe, a first water inlet pipe and an acid inlet pipe, an outlet of the cation exchange column 1 is connected with a first output pipe 3, the first output pipe 3 is connected with a first compressed air pipe, an inlet of the anion exchange column 2 is connected with a second water inlet pipe and an alkali inlet pipe, an outlet of the anion exchange column 2 is connected with a second output pipe 4, the output pipe is connected with a second compressed air pipe, the second output pipe 4 is connected with the first output pipe 3 through a drain pipe and a sugar discharge pipe, the first output pipe 3 is connected with an inlet of the anion exchange column 2 through a connecting pipe 5, an outlet of the cation exchange column 1 is provided with a first low liquid level switch 6, an outlet of the anion exchange column 2 is provided with a second low liquid level switch 7, the first output pipe 3 is also connected with a first backwashing water inlet pipe, and the inlet of the cation exchange column 1 is also connected with a first backwashing water outlet pipe; the second output pipe 4 is also connected with a second backwashing water inlet pipe, the inlet of the anion exchange column 2 is also connected with a second backwashing water outlet pipe, the sugar discharge pipe is connected with a mass flow meter 9, the water discharge pipe is connected with a pH meter 8, and valves V1-V17 are correspondingly arranged on the pipelines.

When the system is normally communicated with liquid, the valves V1, V11 and V17 are opened, the sugar liquid sequentially passes through the cation exchange column 1 and the anion exchange column 2 from top to bottom, and cation and anion impurity ions in the syrup are exchanged with hydrogen ions and hydroxyl ions of resin in the cation and anion exchange columns, so that the impurity ions are removed, and the syrup is purified.

When the exchange of hydrogen ions and hydroxyl ions on the resin reaches the limit, namely the resin is saturated, the resin needs to be regenerated for use. The regeneration process is concretely as follows:

1. sugar discharging: the sugar discharge valves V7 and V14 are opened, and the syrup in the cation exchange column 1 and the anion exchange column 2 flows into the sugar collecting tank by the self gravity until the first low liquid level switch 6 and the second low liquid level switch 7 are indicated to be empty.

2. Stirring by compressed air: keeping sugar discharge valves V7 and V14 open, additionally opening compressed air valves V5 and V16, introducing 1.5bar of compressed air to separate resin and sugar solution, stirring for 15min, and closing V5 and V16.

3. Discharging sugar liquid: when the first low level switch 6, the second low level switch 7 indicate emptying, V7 and V14 are closed simultaneously.

4. Washing and discharging liquid, and collecting sugar liquid in a classified manner: the cation exchange column 1 and the anion exchange column 2 respectively wash residual sugar liquid in the resin by feeding water from a top water inlet valve V2 and a top water inlet valve V9, a sugar discharging valve V7 and a sugar discharging valve V14 are opened, the sugar liquid is sent back to the feeding tank according to the fact that the density of the mass flow meter 9 shows that the sugar liquid is sent back to the feeding tank in a 1.05-1.10g/cm mode, the density of the mass flow meter 9 shows that the sugar liquid is sent back to the sweet water tank in a 1.01-1.05g/cm mode, the density of the mass flow meter 9 shows that the sugar liquid is sent back to the sewer below the 1.01g/cm mode, the water feeding is stopped when the density of the mass flow meter 9 shows that the sugar liquid is sent back to the sweet water tank in a 1.00g/cm mode, namely the water inlet valves V2 and V9 are closed, and the sugar discharging valves V7 and V14 are closed

5. Compressed air agitates the resin: compressed air valves V5 and V16 were opened and 1.5bar of compressed air was admitted to separate the last residual sugar in the resin from the resin, after which V5 and V16 were closed.

6. And (4) washing with water again: opening water inlet valves V2 and V9 at the tops of the cation exchange column 1 and the anion exchange column 2 to wash residual sugar liquid in the resin, opening water discharge valves V8 and V13, discharging little residual sugar in the resin through the water discharge valves, then closing the water inlet valves V2 and V9, and discharging the water discharge valves V8 and V13.

7. Backwashing: opening a backwashing water inlet valve V6 and a backwashing water drain valve V4 at the bottom of the cation exchange column 1, opening a backwashing water inlet valve V15 and a backwashing water drain valve V12 at the bottom of the anion exchange column 2, backwashing until the effluent has no foreign matters such as obvious flocculent protein and the like, and then closing V6, V4, V15 and V12.

8. Acid and alkali regeneration: opening a cation exchange column 1 acid inlet valve V3 and a drain valve V8, opening an anion exchange column 2 alkali inlet valve V10 and a drain valve V13, wherein the concentrations of dilute hydrochloric acid and dilute alkali are 5% and 4% respectively, the regeneration speeds of the dilute acid and the dilute alkali are both 1BV/h, the regeneration volume is 2BV (BV is the volume of resin in the resin column), and then closing V3, V8, V10 and V13.

9. And (3) slow washing: and opening a water inlet valve V2 and a water discharge valve V8 of the cation exchange column 1, opening a water inlet valve V9 and a water discharge valve V13 of the anion exchange column 2, wherein the slow washing speeds of the cation exchange column 1 and the anion exchange column 2 are both 1BV/h, and the regeneration volume is 2BV (BV is the volume of the resin in the resin column). The water quality of the slow washing water is required to be less than 20 mu s/cm, the pH value is 6.5-7.5, and then V3, V8, V10 and V13 are closed

10. Compressed air agitates the resin: compressed air valves V5 and V16 were opened and 1.5bar of compressed air was admitted to separate the last chemical in the resin from the resin, after which V5 and V16 were closed.

11. Quick washing: opening a water inlet valve V2 and a water discharge valve V8 of the cation exchange column 1, opening a water inlet valve V9 and a water discharge valve V13 of the anion exchange column 2, wherein the quick washing speeds of the cation exchange column 1 and the anion exchange column 2 are both 8BV/h, the washing end point is that the pH of the discharged liquid of the cation exchange column 1 is more than 4.0, the pH of the discharged liquid of the anion exchange column 2 is less than 8.0 (BV is the volume of resin in the resin column), and then closing V2, V8, V9 and V13.

12, normal liquid flowing: and opening valves V1, V11 and V17, and after the sugar solution ejects the water in the cation exchange column 1 and the anion exchange column 2, the cation exchange column 1 and the anion exchange column 2 can be normally filled with the liquid.

The system is automatically controlled in operation, manual intervention is few, the whole process can automatically operate after the valve switching time is automatically set, the whole process can be traced, and the regeneration end point judgment is accurate. The resin is stirred by compressed air, so that sugar liquor, chemicals and the resin are fully separated, the sugar liquor, the chemicals and the resin are beneficial to saving water consumption in the processes of water sugar lifting and quick washing, and the water consumption is half of that of the traditional water consumption.

The present invention is not limited to the above embodiments, and based on the technical solutions disclosed in the present invention, those skilled in the art can make some replacements and transformations for some technical features without creative labor according to the disclosed technical contents, and these replacements and transformations are all within the protection scope of the present invention.

Claims

1. The utility model provides a water conservation efficient starch sugar ion exchange system, its characterized in that, includes cation exchange column and anion exchange column, the entry linkage of cation exchange column has into sugar pipe, first inlet tube and into acid tube, the exit linkage of cation exchange column has first output tube, be connected with first compressed air pipe on the first output tube, the entry linkage of anion exchange column has the second inlet tube and advances alkali pipe, the exit linkage of anion exchange column has the second output tube, be connected with second compressed air pipe on the output tube, still link to each other through drain pipe, sugar discharging pipe between second output tube and the first output tube, first output tube passes through the connecting pipe and links to each other with the entry of anion exchange column.

2. The water-saving and efficient starch sugar ion exchange system according to claim 1, wherein a first low liquid level switch is arranged at the outlet of the cation exchange column, and a second low liquid level switch is arranged at the outlet of the anion exchange column.

3. The water-saving high-efficiency starch sugar ion exchange system according to claim 1 or 2, wherein the first output pipe is further connected with a first backwashing water inlet pipe, and the inlet of the cation exchange column is further connected with a first backwashing water outlet pipe; and the second output pipe is also connected with a second backwashing water inlet pipe, and the inlet of the anion exchange column is also connected with a second backwashing water outlet pipe.

4. The water-saving and efficient starch sugar ion exchange system according to claim 1 or 2, wherein a mass flow meter is connected to the sugar discharge pipe, and a pH meter is connected to the water discharge pipe.