CN211913799U - Ion exchange regeneration system - Google Patents
Ion exchange regeneration system Download PDFInfo
- Publication number
- CN211913799U CN211913799U CN202020459054.5U CN202020459054U CN211913799U CN 211913799 U CN211913799 U CN 211913799U CN 202020459054 U CN202020459054 U CN 202020459054U CN 211913799 U CN211913799 U CN 211913799U
- Authority
- CN
- China
- Prior art keywords
- tank
- ion exchange
- regeneration
- ion
- pipeline
- 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
Images
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The utility model relates to an ion exchange regeneration system, which comprises a pre-ion exchange tank, an ion exchange tank, a post-ion exchange storage tank, a waste acid/alkali tank and an acid/alkali preparation tank, the top of the ion exchange tank is provided with a regenerated liquid pipeline which is respectively communicated with the bottoms of the waste acid/alkali tank and the acid/alkali preparation tank, set up the recovery pipeline in the bottom of ion exchange tank respectively with waste acid/alkali jar, the top intercommunication of complex acid/alkali jar, the regeneration liquid in the complex acid/alkali jar gets into the ion exchange jar through the regeneration liquid pipeline and carries out the first soaking regeneration to ion exchange resin, the first regeneration liquid of soaking after the regeneration gets into waste acid/alkali jar through the recovery pipeline and retrieves for use, the first regeneration liquid of storage in waste acid/alkali jar gets into the ion exchange jar through the regeneration liquid pipeline and soaks the regeneration once more to ion exchange resin in, the waste liquid of soaking after the regeneration once more then discharges the ion exchange jar and carries out subsequent processing. The utility model provides the high utilization ratio of spent acid reduces the consumption of spent acid, has reduced the blow off volume of trickle washing water to optimize ion exchange regeneration technology, reduction in production cost.
Description
Technical Field
The utility model belongs to the technical field of the ion exchange regeneration, in particular to ion exchange regeneration system.
Background
The existing sugar alcohol production process usually involves an ion exchange process, and metal ions in materials are removed through the exchange effect of ion exchange resin, so that the product meets the food requirements. When the speed of the ion exchange resin for absorbing metal ions in the sugar solution is balanced with the speed of resolving the metal ions, the ion exchange resin fails and needs to be regenerated by using a regenerant (acid solution or alkali solution), so that the ion exchange resin can be repeatedly used. In the xylose production process, because the corncob hydrolysate contains more impurities, the carbonation flocculation is usually carried out by a carbonic acid method to improve the impurity removal effect, but a large amount of lime is introduced, so that the concentration of calcium ions in the material is as high as 1000-6000 ppm, and the exchange capacity of the ion exchange resin is only 8-10 times of the volume of the resin. Frequent regeneration not only consumes a large amount of regeneration liquid, but also produces a large amount of waste water, thereby restricting the production of enterprises.
In order to reduce the consumption of ion exchange regeneration liquid and reduce sewage discharge, a common method is to optimize the usage amount of a regenerant in a regeneration process, so that the unit consumption of the regenerant per ton of products is the lowest, and simultaneously, the standard of a resin leaching end point is reduced to achieve the purpose of reducing sewage discharge. However, the method has the following disadvantages: 1. because the using amount of the regenerant is controlled, when the property of the ion exchange sugar solution fluctuates, the phenomenon of incomplete regeneration is easy to occur, so that the ion exchange amount is unstable, and the concentration fluctuation of the produced ion exchange solution is high; 2. the use amount of the regenerant is controlled for a long time, so that the pollution degree of the ion-exchange resin is higher and higher, and the ion-exchange resin needs to be periodically recovered; 3. the elution key standard of the ion-exchange resin is reduced during regeneration, so that the environment of the sugar solution is peracid or overbase when the ion-exchange resin is used for the second time, and the adverse effects such as isomerization, yellowing of color and the like are easy to occur.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem, the utility model provides an ion exchange regeneration system, use excessive regenerant in the ion exchange resin regeneration process, improve the exchange capacity of ion exchange resin, useless regenerant recovery system has been established simultaneously, retrieve excessive part regenerant, be used for the regeneration process of ion exchange resin next time, thereby reach the purpose that reduces the regenerant unit consumption, on the other hand is in order to reduce the ion exchange regeneration sewage discharge, ion exchange wastewater recovery system has been established, the waste water that produces the ion exchange resin washing back section in the ion exchange regeneration process is retrieved, be used for disposing the regenerant, thereby reach and reduce sewage discharge and reduce the dual effect of regenerant configuration water consumption.
The utility model is realized in this way, the utility model provides an ion exchange regeneration system, which comprises an ion exchange front tank, an ion exchange rear storage tank, a waste acid/alkali tank and an acid/alkali distribution tank, wherein the ion exchange tank is internally provided with ion exchange resin for carrying out ion exchange treatment on sugar liquor to be subjected to ion exchange conveyed from the ion exchange front tank, the ion exchange rear storage tank stores ion exchange liquid with high sugar concentration after ion exchange, the top of the ion exchange tank is respectively provided with a normal blowing pipeline for introducing compressed air and a normal washing pipeline for introducing purified water, the bottom of the ion exchange tank is respectively provided with a back blowing pipeline for introducing compressed air and a back washing pipeline for introducing purified water, the top of the ion exchange tank is also provided with a regeneration liquid pipeline which is respectively communicated with the waste acid/alkali tank and the bottom of the acid/alkali distribution tank, the bottom of the ion exchange tank is also provided with a recovery pipeline which is respectively communicated with the waste acid/alkali tank and the top of the acid/alkali distribution tank, the regeneration liquid stored in the acid/alkali preparation tank enters the ion exchange tank through regeneration liquid pipelines respectively to carry out primary soaking regeneration on the ion exchange resin, the primary regeneration liquid after primary soaking regeneration enters the waste acid/alkali preparation tank through a recovery pipeline to be recovered for standby use, the primary regeneration liquid stored in the waste acid/alkali preparation tank enters the ion exchange tank through the regeneration liquid pipeline to carry out secondary soaking regeneration on the ion exchange resin, the waste liquid after secondary soaking regeneration is discharged out of the ion exchange tank to carry out subsequent treatment, purified water is used for leaching the regenerated ion exchange resin through a forward washing pipeline, and the leached washing water enters the acid/alkali preparation tank through the recovery pipeline to prepare the pH of acid liquor/alkali liquor in the acid/alkali preparation tank.
Furthermore, an upper sewage discharge pipeline and a lower sewage discharge pipeline are respectively arranged at the upper part and the bottom of the ion exchange tank, sewage generated after the ion exchange resin is positively washed by purified water is discharged through the lower sewage discharge pipeline, sewage generated after the ion exchange resin is reversely washed is discharged through the upper sewage discharge pipeline, and waste liquid generated after the ion exchange resin is soaked again and regenerated is also discharged through the lower sewage discharge pipeline.
Furthermore, the ion exchange regeneration system further comprises a sweet water tank, the bottom of the ion exchange tank is respectively provided with a sweet water pipeline communicated with the sweet water tank and a liquid outlet pipeline communicated with the storage tank after ion exchange, the sweet water tank collects sugar liquid (namely low-concentration ion exchange liquid) with low sugar concentration temporarily stored in the ion exchange tank before ion exchange resin is regenerated through the sweet water pipeline, and the ion exchange liquid with high sugar concentration temporarily stored in the storage tank after ion exchange is entered through the liquid outlet pipeline.
Furthermore, a liquid inlet pipeline communicated with the ion exchange front tank is arranged at the top of the ion exchange tank, and a liquid inlet valve, a liquid inlet pump and a liquid inlet flowmeter are respectively arranged on the liquid inlet pipeline.
Further, a regeneration pump and a regeneration liquid flow meter are arranged on the regeneration liquid pipeline.
Furthermore, an acid/alkali input pipeline for supplementing concentrated acid liquid/alkali liquid into the tank and a purified water input pipeline for adjusting the pH value of the acid liquid/alkali liquid in the tank are also arranged on the acid/alkali preparation tank.
Furthermore, control valves are respectively arranged on the forward blowing pipeline, the forward washing pipeline, the back blowing pipeline, the back washing pipeline, the regenerated liquid pipeline and the recovery pipeline.
Compared with the prior art, the utility model discloses an ion exchange regeneration system has following characteristics:
1. ensuring the regeneration thoroughness of the ion-exchange resin, reducing the recovery period of the ion-exchange resin and improving the production continuity;
2. the excessive acid/alkali is recycled, so that the utilization rate of the regenerant is improved, and the unit consumption of the regenerant is reduced;
3. the waste water recovery system is established, so that the water supplementing amount in the preparation process of the regenerant is greatly reduced, the production water consumption is reduced, and the discharge amount of the regenerated sewage is reduced.
Drawings
Fig. 1 is a schematic structural diagram of a preferred embodiment of the present invention.
Detailed Description
In order to make the technical problem, technical solution and advantageous effects to be solved by the present invention more clearly understood, the following description is given in conjunction with the accompanying drawings and embodiments to illustrate the present invention in further detail. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Referring to fig. 1, the preferred embodiment of the ion-exchange regeneration system of the present invention comprises a pre-ion-exchange tank 1, an ion-exchange tank 4, a sweet water tank 5, a post-ion-exchange storage tank 6, a waste acid/alkali tank 12, and a complex acid/alkali tank 13. The arrows in the figure show the flow direction of the materials (sugar solution, purified water, compressed air, acid solution, alkali solution, regenerated solution, ion exchange solution, sewage and the like) in the system.
The pre-ion-exchange tank 1 comprises a tank body, a stirring device, a liquid level meter and the like and is used for storing sugar liquid before ion-exchange treatment. The ion exchange tank 4 comprises a storage tank, wherein ion resin, quartz sand, a liquid level meter, a tuning fork switch, a thermometer and the like are arranged in the storage tank, and the ion exchange resin is used for carrying out ion exchange treatment on the sugar solution to be subjected to ion exchange conveyed from the tank before ion exchange. The sweet water tank 5 comprises a storage tank, a liquid level meter and the like and is used for temporarily storing the sugar-topped water before ion exchange regeneration and the sugar liquid with low sugar content and low concentration generated by the sugar-topped water before ion exchange use. The storage tank 6 after ion exchange comprises a storage tank, a stirring device, a liquid level meter and the like and is used for storing the ion exchange liquid with high sugar concentration after ion exchange. The spent acid/base tank 12 is used to recover excess acid/base from the ion exchange regeneration process. The complex acid/alkali tank 13 is used for configuring acid/alkali required in the ion exchange regeneration process.
The top of the ion exchange tank 4 is provided with a liquid inlet pipeline A communicated with the ion exchange front tank 1, and the liquid inlet pipeline A is respectively provided with a liquid inlet valve 2, a liquid inlet pump 9 and a liquid inlet flowmeter 3. The sugar liquid to be ion-exchanged in the pre-ion-exchange tank 1 enters the ion-exchange tank 4 through a liquid inlet valve 2 and a liquid inlet flowmeter 3 under the drive of a liquid inlet pump 9. The liquid inlet valve 2 is used for controlling the feeding flow of the ion exchange tank 4. The liquid inlet flowmeter 3 comprises a flowmeter online monitoring system and is used for online monitoring the flow of the sugar solution to be subjected to ion exchange.
The top of the ion exchange tank 4 is respectively provided with a positive blowing pipeline B for introducing compressed air and a positive washing pipeline C for introducing purified water, and the bottom of the ion exchange tank 4 is respectively provided with a back blowing pipeline D for introducing compressed air and a back washing pipeline E for introducing purified water. A valve 17 is arranged on the forward blowing pipeline B, a valve 16 is arranged on the forward washing pipeline C, a valve 18 is arranged on the back blowing pipeline D, and a valve 19 is arranged on the back washing pipeline E. Valves 17 and 18 are used to control the opening and closing of the compressed air. Valves 16 and 19 are used to regulate the purified water feed flow.
The top of the ion exchange tank 4 is also provided with a regenerated liquid pipeline F which is respectively communicated with the bottoms of the waste acid/alkali tank 12 and the acid/alkali preparation tank 13, and the bottom of the ion exchange tank 4 is also provided with a recovery pipeline G which is respectively communicated with the tops of the waste acid/alkali tank 12 and the acid/alkali preparation tank 13. The regeneration liquid (the regeneration liquid is acid liquid/alkali liquid with certain pH value) stored in the acid/alkali preparation tank 13 respectively enters the ion exchange tank 4 through the regeneration liquid pipeline F to carry out primary soaking regeneration on the ion exchange resin, and the primary regeneration liquid after the primary soaking regeneration enters the waste acid/alkali tank 12 through the recovery pipeline G to be recovered for later use. The primary regeneration liquid stored in the waste acid/alkali tank 12 enters the ion exchange tank 4 through the regeneration liquid pipeline F to perform soaking regeneration on the ion exchange resin again, and the waste liquid after soaking regeneration again is discharged out of the ion exchange tank 4 for subsequent treatment. The ion exchange resin regeneration liquid is prepared, so that the regeneration thoroughness of the ion exchange resin is ensured, the recovery period of the ion exchange resin is reduced, and the production continuity is improved. On the other hand, the excessive acid/alkali is recycled, so that the utilization rate of the regenerant is improved, and the effect of reducing the unit consumption of the regenerant is realized.
The regenerated ion exchange resin is leached by external purified water through a forward washing pipeline C, and the leached leaching water enters the acid/alkali preparation tank 13 through a recovery pipeline G so as to prepare the pH value of acid liquor/alkali liquor in the acid/alkali preparation tank, so that the water supplement amount is reduced, the purpose of reducing the production water consumption is achieved, and the effect of reducing the discharge amount of regenerated sewage is achieved.
A regeneration pump 11 and a regeneration liquid flow meter 10 are provided on the regeneration liquid line F. A valve 14 is arranged on a recovery pipeline G communicated with the waste acid/alkali tank 12, and a valve 15 is arranged on a recovery pipeline G communicated with the acid/alkali preparation tank 13. A valve 23 is arranged on a regenerated liquid pipeline F communicated with the waste acid/alkali tank 12, and a valve 22 is arranged on a regenerated liquid pipeline F communicated with the acid/alkali preparation tank 13. The regeneration fluid flow meter 10 is used to monitor the flow of regeneration fluid into the ion exchange regeneration process. Valve 14 and valve 15 are used to control the recovery of spent acid/alkali, waste water in the ion exchange regeneration process, respectively. Valve 22 controls the discharge flow of neo-acid/base. Valve 23 controls the flow of spent acid/base in and out.
An upper sewage discharge pipeline H and a lower sewage discharge pipeline J are respectively arranged at the upper part and the bottom of the ion exchange tank 4 and communicated with a sewage station. The purified water discharges the sewage after the ion exchange resin is positively washed through a lower sewage discharge pipeline J, and the sewage after the ion exchange resin is reversely washed is discharged through an upper sewage discharge pipeline H. The waste liquid after the ion exchange resin is soaked again and regenerated is also discharged through a lower sewage discharge pipeline J. A valve 21 is arranged on the upper sewage discharge pipeline H, and a valve 20 is arranged on the lower sewage discharge pipeline J. The valve 20 controls the opening and closing of the ion-exchange lower sewage draining pipeline J. The valve 21 is used for controlling the opening and closing of the ion upper sewage discharge pipeline H.
The bottom of the ion exchange tank 4 is also respectively provided with a sweet water pipeline K communicated with the sweet water tank 5 and a liquid outlet pipeline L communicated with the storage tank 6 after ion exchange. The sweet water tank 5 collects sugar liquid with low sugar concentration (i.e. low-concentration ion exchange liquid) temporarily stored in the ion exchange tank 4 before ion exchange resin is regenerated through a sweet water pipeline K, and the ion exchange liquid with high sugar concentration enters the post-ion exchange storage tank 6 through a liquid outlet pipeline L for storage. A valve 7 is arranged on the sweet water pipeline K, and a valve 8 is arranged on the liquid outlet pipeline L. The valve 7 and the valve 8 are used for controlling the discharge direction in the ion exchange regeneration process.
The acid/alkali preparation tank 13 is also provided with an acid/alkali input pipeline M for supplementing concentrated acid liquid/alkali liquid into the tank and a purified water input pipeline N for adjusting the pH value of the acid liquid/alkali liquid in the tank.
In the above valves, the liquid inlet valve 2, the valve 16, the valve 19, the valve 22 and the valve 23 are pneumatic control valves, the valve 7, the valve 8, the valve 17, the valve 18 and the valve 20 are pneumatic switch valves, and the valve 14 and the valve 15 are pneumatic valves.
The ion exchange regeneration system of the present invention will be further described with reference to the following specific embodiments.
Taking the regeneration process of the xylose ion-exchange column as an example for illustration, the volume of the ion-exchange resin in the ion-exchange tank 4 is 6m for carrying out the cultivation, the refraction of the ion-exchange sugar liquid is 50 +/-2%, and the feeding flow is 5m for carrying out the cultivation/h.
Step one, water-topped sugar: and when the discharge detection result of the ion exchange column exceeds the requirement, judging that the ion exchange resin in the ion exchange tank 4 needs to be regenerated. Closing the valve 2 and the liquid inlet pump 9, opening a valve 16 of purified water, adding the purified water into the ion exchange tank 4 at a feeding flow rate of 5 m/h, jacking the sugar liquid in the ion exchange tank 4 into the storage tank 6 after ion exchange, closing the valve 8 when the discharge concentration is lower than 40%, opening the valve 7, jacking the residual materials in the ion exchange tank 4 into the sweet water tank 5 until the discharge concentration is detected to be 0.
Second step, back flushing and back washing: close valve 7 and valve 16, open valve 18, it is loose with the ion exchange resin blowback of compressed air in with the ion exchange jar 4, prevent that long-time operation from the hardening of ion exchange resin appearance, time control is at 10~15min, after the blowback, close valve 18, open valve 19 and valve 21, purified water is good at with flow 24m and is adorned the ion exchange resin for 20min, and backwash sewage discharges to the sewage station through last sewage pipes H.
Step three, liquid level reduction: after the backwashing is finished, the valve 20 is opened to reduce the liquid level to a position 10cm above the resin exchange layer, and the backwashing sewage is discharged to a sewage station through a lower sewage discharge pipeline J.
Step four, primary regeneration: and closing the valve 19 and the valve 21, opening the regeneration liquid flowmeter 10, the regeneration pump 11, the valve 20 and the valve 23, carrying out tophan/h on the waste acid in the waste acid tank 12 through a regeneration liquid pipeline F at a flow rate of 12m, injecting the waste acid into the ion exchange tank 4, and closing the regeneration liquid flowmeter 10, the regeneration pump 11, the valve 20 and the valve 23 after the completion of the tophan process for soaking for 30 min. And discharging the waste liquid after the primary regeneration to a sewage station through a lower sewage discharge pipeline J.
Step five, secondary regeneration: opening the regeneration liquid flow meter 10, the regeneration pump 11 and the valve 22, adding the prepared fresh acid into the ion exchange tank 4 through the regeneration liquid pipeline F at the flow rate of 12 m/h, feeding the acid for 1 hour, closing the regeneration liquid flow meter 10, the regeneration pump 11 and the valve 22 after the completion of the acid feeding, and soaking for 2 hours.
Sixth step, recovering waste acid and alkali: after soaking, open valve 14 and valve 16, pour into 12 m/h flow purification water into from handing over jar 4 and carry out the sour alkali after soaking and push into waste acid jar 12 through recovery pipeline G and retrieve temporarily to be used for in the next regeneration process of ion-exchange resin.
Step seven, leaching: and after the acid-base recovery is finished, opening the valve 20, closing the valve 14, leaching the regenerated ionic resin in the ion exchange tank 4 by using 36 m/h flow purified water, and leaching for 2 hours.
Eighth step, standby: and when the leaching time is 1.5h, opening the valve 15, closing the valve 20, recovering the leaching wastewater for the last half hour through the recovery pipeline G for preparing the regenerated acid liquor, and closing the valve 15 after the recovery is finished. And after leaching, detecting the pH value and the conductivity of the discharged material, and reducing the liquid level in the ion exchange tank 4 to a position 10cm above the ion exchange resin for later use after the requirement is met.
The recycling of waste acid and waste water generated in the process of regenerating the ion-exchange resin is completed through the eight steps, the utilization rate of the waste acid is improved, the consumption of the waste acid is reduced, and the discharge capacity of the shower water is reduced, so that the aim of optimizing the ion-exchange regeneration process is fulfilled, and the production cost is reduced.
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (7)
1. An ion exchange regeneration system is characterized by comprising a pre-ion exchange tank, an ion exchange tank, a post-ion exchange storage tank, a waste acid/alkali tank and an acid/alkali preparation tank, wherein the ion exchange tank is internally provided with ion exchange resin for carrying out ion exchange treatment on sugar solution to be ion exchanged conveyed from the pre-ion exchange tank, the post-ion exchange storage tank is used for storing ion exchange liquid with high sugar content concentration after ion exchange, the top of the ion exchange tank is respectively provided with a forward blowing pipeline for introducing compressed air and a forward washing pipeline for introducing purified water, the bottom of the ion exchange tank is respectively provided with a reverse blowing pipeline for introducing compressed air and a reverse washing pipeline for introducing purified water, the top of the ion exchange tank is also provided with a regeneration liquid pipeline which is respectively communicated with the bottoms of the waste acid/alkali tank and the acid/alkali preparation tank, the bottom of the ion exchange tank is also provided with a recovery pipeline which is respectively communicated with the tops of the waste acid/alkali preparation tank and the acid/alkali preparation tank, and the regeneration liquid stored in the acid/alkali preparation tank enters the ion exchange tank through regeneration liquid pipeline respectively to carry out the And (2) secondary soaking regeneration, wherein primary regenerated liquid after primary soaking regeneration enters a waste acid/alkali tank through a recovery pipeline to be recovered for standby application, primary regenerated liquid stored in the waste acid/alkali tank enters the ion exchange tank through a regenerated liquid pipeline to carry out secondary soaking regeneration on the ion exchange resin, waste liquid after secondary soaking regeneration is discharged from the ion exchange tank to carry out subsequent treatment, purified water leaches the regenerated ion exchange resin through a forward washing pipeline, and the leached water enters the acid/alkali preparation tank through the recovery pipeline to prepare the pH value of acid liquor/alkali liquor in the acid/alkali preparation tank.
2. The ion-exchange regeneration system according to claim 1, wherein an upper sewage drain line and a lower sewage drain line are further provided at the upper part and the bottom part of the ion-exchange tank, respectively, the sewage after the purified water is used for positively washing the ion-exchange resin is discharged through the lower sewage drain line, the sewage after the purified water is used for reversely washing is discharged through the upper sewage drain line, and the waste liquid after the ion-exchange resin is soaked again is also discharged through the lower sewage drain line.
3. The ion-exchange regeneration system of claim 1, further comprising a sweet water tank, wherein a sweet water pipeline communicated with the sweet water tank and a liquid outlet pipeline communicated with the post-ion storage tank are respectively arranged at the bottom of the ion-exchange tank, the sweet water tank collects sugar solution with low sugar concentration temporarily stored in the ion-exchange tank before the ion-exchange resin is regenerated through the sweet water pipeline, and the ion-exchange solution with high sugar concentration enters the post-ion storage tank through the liquid outlet pipeline for storage.
4. The ion-exchange regeneration system as claimed in claim 1, wherein the top of the ion-exchange tank is provided with a liquid inlet pipeline communicated with the pre-ion-exchange tank, and a liquid inlet valve, a liquid inlet pump and a liquid inlet flowmeter are respectively arranged on the liquid inlet pipeline.
5. The ion-exchange regeneration system of claim 1, wherein a regeneration pump and a regeneration fluid flow meter are disposed on the regeneration fluid line.
6. The ion exchange regeneration system of claim 1, wherein an acid/alkali input line for replenishing the concentrated acid/alkali solution in the tank and a purified water input line for adjusting the pH of the acid/alkali solution in the tank are further provided in the acid/alkali preparation tank.
7. The ion-exchange regeneration system of claim 1, wherein control valves are respectively disposed on the forward blowing pipeline, the forward washing pipeline, the reverse blowing pipeline, the reverse washing pipeline, the regeneration liquid pipeline and the recovery pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020459054.5U CN211913799U (en) | 2020-04-01 | 2020-04-01 | Ion exchange regeneration system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020459054.5U CN211913799U (en) | 2020-04-01 | 2020-04-01 | Ion exchange regeneration system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211913799U true CN211913799U (en) | 2020-11-13 |
Family
ID=73349044
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020459054.5U Active CN211913799U (en) | 2020-04-01 | 2020-04-01 | Ion exchange regeneration system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211913799U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112410474A (en) * | 2020-11-16 | 2021-02-26 | 南京甘汁园糖业有限公司 | Ion exchange decoloration water-saving process for refined sugar |
| CN112723675A (en) * | 2020-12-26 | 2021-04-30 | 浙江华康药业股份有限公司 | Ion exchange regeneration sewage calcium removal system and method |
| CN113976186A (en) * | 2021-11-25 | 2022-01-28 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
| CN115555055A (en) * | 2021-07-01 | 2023-01-03 | 中粮糖业辽宁有限公司 | Resin regeneration system and resin regeneration method |
-
2020
- 2020-04-01 CN CN202020459054.5U patent/CN211913799U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112410474A (en) * | 2020-11-16 | 2021-02-26 | 南京甘汁园糖业有限公司 | Ion exchange decoloration water-saving process for refined sugar |
| CN112410474B (en) * | 2020-11-16 | 2023-09-15 | 南京甘汁园股份有限公司 | Ion exchange decoloring water-saving process for refining sugar |
| CN112723675A (en) * | 2020-12-26 | 2021-04-30 | 浙江华康药业股份有限公司 | Ion exchange regeneration sewage calcium removal system and method |
| CN115555055A (en) * | 2021-07-01 | 2023-01-03 | 中粮糖业辽宁有限公司 | Resin regeneration system and resin regeneration method |
| CN113976186A (en) * | 2021-11-25 | 2022-01-28 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
| CN113976186B (en) * | 2021-11-25 | 2023-08-15 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN211913799U (en) | Ion exchange regeneration system | |
| CN101357794B (en) | Ion-exchange process technique of hexavalent chrome-containing waste water | |
| CN112062796B (en) | Acarbose continuous desalting and neutralizing production method based on continuous ion exchange device | |
| CN106350614A (en) | Comprehensive recycling method for preparing hybridization water and acid-base by utilizing malt syrup | |
| CN212655517U (en) | Dual-mode switching operation metallurgical wastewater softening device | |
| CN113476942A (en) | Filter backwashing system, process and control method | |
| CN114277197A (en) | Method for softening beet syrup | |
| CN211585316U (en) | System for continuously removing anions in 3-hydroxy-1, 3, 5-pentanedioic acid | |
| CN216890255U (en) | Acid-base wastewater neutralization treatment system for chinlon slice production process | |
| CN101367569B (en) | Ion exchange treatment process for cyanide containing wastewater | |
| CN216368017U (en) | Xylose mother liquor ion exchange system | |
| CN211688289U (en) | Device for removing impurity ions in lithium sulfate solution | |
| CN109201123A (en) | A kind of method that ion exchange resin regeneration ffluent recycles | |
| CN113499805A (en) | Method for regenerating purifying column of ultrapure water purifier | |
| CN102863054A (en) | Device for classification recycling of ion exchange resins and process thereof | |
| CN104003477A (en) | External regeneration reverse-flow ion exchange system and application method thereof | |
| CN111068361B (en) | Caprolactam ion exchange device and regeneration method thereof | |
| CN214572048U (en) | Water-saving and efficient starch sugar ion exchange system | |
| CN203839061U (en) | Reverse osmosis boron concentrating device for waste liquid processing system of nuclear power plant | |
| CN219217641U (en) | Resin softening tank | |
| CN219730620U (en) | Exchange resin desalination device for reducing strong brine | |
| CN215975081U (en) | Full-automatic water softener | |
| CN109502693A (en) | A kind of full-automatic softening plant and method applied to Treated sewage reusing processing system | |
| CN217473555U (en) | Fructose ion exchange switching system | |
| CN220926376U (en) | Ion exchange softened water treatment equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |