CN112295610A - Chelate resin regeneration process in secondary brine refining process - Google Patents
Chelate resin regeneration process in secondary brine refining process Download PDFInfo
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/50—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/60—Cleaning or rinsing ion-exchange beds
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Abstract
The invention provides a chelate resin regeneration process in a secondary brine refining process, which is characterized by comprising the following steps of: the method comprises the following process steps: draining, bubbling and settling. Further, the method comprises the steps of draining brine, backwashing, primary draining, primary acid washing, primary bubbling, primary settling, draining waste acid liquor, primary washing, secondary bubbling, secondary settling, secondary draining, alkali washing, tertiary bubbling, tertiary settling, draining alkaline water, secondary washing, quaternary bubbling, quaternary settling, tertiary draining and filling brine in sequence. The washing effect is ensured, the consumption of pure water is greatly reduced, the consumption of sodium hydroxide is reduced, and the generation amount of waste water is reduced.
Description
Technical Field
The invention relates to a chelate resin regeneration process in a secondary brine refining process, which mainly relates to a chelate resin regeneration process in the secondary brine refining process in the caustic soda preparation process by ionic membrane electrolysis.
Background
The operation mode of the resin tower is as follows: the two towers are connected in series, one main tower and one auxiliary tower are in on-line normal operation, and the other tower is in off-line isolation for resin regeneration. After the main tower is regenerated on the lower line, the auxiliary tower rises to be the main tower, and the regeneration tower is regenerated on the upper line to be the auxiliary tower. In order to enhance the activity of the resin and ensure that the quality of the brine entering the electric cell continuously meets the standard for a long time and is qualified, the resin which adsorbs a large amount of multivalent cations in the offline tower (used as a main tower) needs to be regenerated and reduced by using hydrochloric acid and caustic soda in a circulating way every 72 hours. The switching of the ion exchange column and the regeneration and reduction of the resin are automatically performed according to a design program. In the resin regeneration process, a large amount of acid/alkali/salt/wastewater can be generated, the environmental protection pressure is increased, and the consumption of materials such as acid, alkali, pure water and the like is increased.
The prior art consumes large amount of alkali and water, and further generates a large amount of waste water, so that the material consumption is serious, and the environmental protection pressure is caused.
Disclosure of Invention
The invention aims to provide a chelate resin regeneration process in a secondary brine refining process, which achieves the following aims: the consumption of materials such as caustic soda, pure water and the like is reduced, and the environmental protection pressure brought by wastewater treatment is reduced.
In order to achieve the purpose, the following technical scheme is adopted:
the invention relates to a chelate resin regeneration process in a secondary brine refining process, which aims at a resin tower in the secondary brine refining process in an ionic membrane electrolysis caustic soda manufacturing process, wherein the resin tower is a vertical cylindrical tower body with an upper end socket and a lower end socket, the full volume is 40-80m for cultivating a tree, the diameter of the tower body is 3-5 m, and the height of the cylindrical tower body is 3-4 m. The resin is positioned on the upper part of the water cap of the cylindrical tower body of the resin tower and has the height of 1-1.5 m.
The resin regeneration process comprises the following steps:
a. draining saline water: the salt water in the resin tower is discharged by pure instrument wind of 0.5-0.7MPa, and preparation is made for pure water backwashing the resin.
Controlling the instrument air flow rate to be 18-22 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the salt water in the tower is drained and automatically entering the next step.
b. Backwashing: the compressed resin layer is loosened with pure water, and backwashed pure water is supplied from the bottom of the resin column.
Controlling the backwashing pure water flow rate to be 50-70 m/h, and controlling the backwashing time to be 25-40 min. And automatically entering the next step after the time is up.
c. And (4) primary drainage, namely draining the cleaning water in the resin tower by using instrument gas.
Controlling the gas flow of the instrument to be 18-22 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the backwash water in the tower is drained and automatically entering the next step.
d. And (3) primary acid washing, namely eluting the substances adsorbed on the resin by using a diluted hydrochloric acid solution. Hydrochloric acid with the mass concentration of 18% is diluted by pure water through a mixer to obtain a dilute hydrochloric acid solution with the concentration of about 7% after dilution. The dilute hydrochloric acid solution is delivered to the resin layer from the upper distribution pipe of the resin tower, and the waste water is discharged from the lower part of the tower.
Carrying out the dry-mass-concentration 18% ethanol-liquid separation on the obtained dry-mass-concentration ethanol-liquid separation and the obtained dry-mass-concentration ethanol-liquid separation, wherein the flow of hydrochloric acid with the mass concentration of 18% is 14-15 m/h, the flow of pure water is 24-25 m/h, the pickling time is 50-70 min, and the next step is automatically carried out after the pickling time is.
e. Primary bubbling: after completion of the acid washing, the resin was thoroughly contacted with hydrochloric acid by bubbling with instrument gas. Instrumentation gas enters from the bottom of the column.
Controlling the gas flow rate of the instrument for bubbling to be 18-22 Nm/h for 10-15 minutes, and automatically entering the next step after the time.
f. And (4) primary sedimentation, namely standing and settling the resin layer boiled due to bubbling. The settling time was 100-150 minutes.
g. And (3) discharging waste acid liquid, namely discharging the dilute hydrochloric acid solution in the resin tower by using instrument gas, wherein the instrument gas enters from the top of the resin tower, and the waste water is discharged from the bottom of the resin tower.
And controlling the gas flow of the instrument to be 18-22 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the waste water in the tower is drained and automatically entering the next step.
h. And (4) primary water washing, namely washing the residual hydrochloric acid solution in the resin tower by using pure water. Pure water is delivered to the resin layer from the upper distribution pipe of the resin tower, and waste water is discharged from the bottom of the resin tower.
Controlling the flow of pure water for washing to be 45-50m for carrying out the cultivation under the condition of 20-40 minutes. And automatically entering the next step after the time is up.
i. And (4) secondary bubbling, namely bubbling with instrument gas to ensure that the resin is fully contacted with pure water. The instrument gas enters from the bottom of the resin tower.
Controlling the gas flow rate of the instrument for bubbling to be 18-22 Nm/h for 10-15 minutes, and automatically entering the next step after the time.
j. And (4) secondary sedimentation, namely standing and settling the resin layer boiled due to bubbling.
The standing time is 10-15 minutes, and the next step is automatically carried out after the standing time.
k. And (4) secondary drainage, namely discharging the washing wastewater in the resin tower by using instrument gas.
And controlling the gas flow of the instrument to be 18-22 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the waste water in the tower is drained and automatically entering the next step.
In order to wash and discharge all the hydrochloric acid remaining in the resin, the steps of h washing, i bubbling, j settling and k draining were repeated once.
And l, alkali washing, namely diluting a sodium hydroxide solution with the mass concentration of 32% to a dilute sodium hydroxide solution with the mass concentration of about 4% by a mixer with pure water. The dilute sodium hydroxide solution is fed into the resin layer from the upper distribution pipe of the resin tower, and the weak base water is discharged from the bottom of the resin tower.
Controlling the flow rate of the sodium hydroxide solution with the mass concentration of 32% to be 3-4 m/h, controlling the flow rate of pure water to be 35-36 m/h, controlling the alkali washing time to be 80-100 minutes, and automatically carrying out the next step after the time comes.
And m, bubbling for three times, namely bubbling with instrument gas to ensure that the resin layer is in full contact reaction with alkali liquor, and the instrument gas enters from the bottom of the tower.
Controlling the gas flow rate of the instrument for bubbling to be 18-22 Nm/h for 10-15 minutes, and automatically entering the next step after the time.
And n, settling for three times, namely standing and settling the resin layer boiled due to bubbling.
Standing for 20-30 minutes, and automatically entering the next step after the time is up.
And o, discharging alkali water, namely discharging the dilute alkali water in the resin tower by using instrument gas.
And controlling the gas flow of the instrument to be 18-22 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the waste water in the tower is drained and automatically entering the next step.
And p, secondary water washing, namely washing the residual caustic soda solution in the resin tower by using pure water. Pure water enters from the upper distribution pipe of the resin tower, and waste water is discharged from the bottom of the tower.
Controlling the flow of pure water for washing to be 45-50m and carrying out the downward cultivation for 20-30 min, and automatically carrying out the next step after the flow is reached.
And q, bubbling for four times, namely bubbling with instrument gas to ensure that the resin is fully contacted with pure water, wherein the instrument gas enters from the bottom of the resin tower.
Controlling the gas flow rate of the instrument for bubbling to be 18-22 Nm/h for 10-15 minutes, and automatically entering the next step after the time.
And r, four times of sedimentation, namely standing and settling the resin layer boiled due to bubbling.
The settling time is 10-15 minutes, and the next step is automatically carried out after the settling time.
s. tertiary drainage: and discharging the weak alkaline water in the resin tower by instrument gas.
And controlling the gas flow of the instrument to be 18-22 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the waste water in the tower is drained and automatically entering the next step.
And t, filling salt water, namely enabling refined salt water to enter and fill the resin tower. The salt water enters from the bottom of the resin tower, and the waste water is discharged from the top of the resin tower.
And (3) filling the resin tower with qualified refined brine processed by the resin tower, and controlling the brine flow to be 30-40m for carrying out the cultivation/h and the time to be 80-100 minutes.
The regeneration of the resin tower is completed.
By adopting the technical scheme, the invention has the beneficial effects that:
the traditional process steps for resin tower regeneration are as follows: the method comprises the steps of water washing, backwashing, acid washing, water washing, alkali washing, water washing and brine replacement, and the traditional process ensures the water washing effect, has long water washing time and large water consumption and large sodium hydroxide consumption. The invention adds the steps of bubbling, settling and draining by instrument gas, and is matched with other steps, thereby not only ensuring the washing effect, but also greatly reducing the use amount of pure water, and reducing the use amount of sodium hydroxide while ensuring the washing effect through twice washing of the resin after acid washing, and reducing the use amount of the sodium hydroxide by more than 15%; the production amount of the waste water is reduced by about 50 percent; has good economic benefit and environmental protection benefit.
Detailed Description
Example 1 Process for regenerating chelate resin in Secondary brine refining Process
The regeneration process is a resin tower aiming at the secondary brine refining process in the process of preparing caustic soda by ionic membrane electrolysis, the resin tower is a vertical cylindrical tower body with an upper end cap and a lower end cap, the full volume is 57m, the diameter of the tower body is 4 meters, and the height of the cylindrical tower body is 3.14 meters. The resin is positioned on the upper part of the water cap of the cylindrical tower body of the resin tower and has the height of 1.3-1.4 meters.
The resin regeneration process comprises the following steps:
a. draining saline water: the brine in the resin tower was discharged with 0.6MPa clean meter air in preparation for pure water backwashing the resin.
And controlling the instrument air flow to be 20 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the salt water in the tower is drained and automatically entering the next step.
b. Backwashing: the compressed resin layer is loosened with pure water, and backwashed pure water is supplied from the bottom of the resin column.
Controlling the backwashing pure water flow at 60 m/h and the backwashing time at 30 minutes. And automatically entering the next step after the time is up.
c. And (4) primary drainage, namely draining the cleaning water in the resin tower by using instrument gas.
And controlling the gas flow of the instrument to be 20 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the backwashing water in the tower is drained and automatically entering the next step.
d. And (3) primary acid washing, namely eluting the substances adsorbed on the resin by using a diluted hydrochloric acid solution. Hydrochloric acid with the mass concentration of 18% is diluted by pure water through a mixer to obtain a dilute hydrochloric acid solution with the concentration of about 7% after dilution. The dilute hydrochloric acid solution is delivered to the resin layer from the upper distribution pipe of the resin tower, and the waste water is discharged from the lower part of the tower.
And carrying out the following steps automatically after the pickling time is 60 minutes, wherein the hydrochloric acid flow rate with the mass concentration of 18% is 14.37m and the pure water flow rate is 24.63 m.
e. Primary bubbling: after completion of the acid washing, the resin was thoroughly contacted with hydrochloric acid by bubbling with instrument gas. Instrumentation gas enters from the bottom of the column.
And controlling the gas flow rate of the instrument for bubbling to be 20 Nm/h for 12 minutes, and automatically entering the next step after the time.
f. And (4) primary sedimentation, namely standing and settling the resin layer boiled due to bubbling. The settling time was 120 minutes.
g. And (3) discharging waste acid liquid, namely discharging the dilute hydrochloric acid solution in the resin tower by using instrument gas, wherein the instrument gas enters from the top of the resin tower, and the waste water is discharged from the bottom of the resin tower.
And controlling the gas flow of the instrument to be 20 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the waste water in the tower is drained, and automatically entering the next step.
h. And (4) primary water washing, namely washing the residual hydrochloric acid solution in the resin tower by using pure water. Pure water is delivered to the resin layer from the upper distribution pipe of the resin tower, and waste water is discharged from the bottom of the resin tower.
Controlling the flow of pure water for washing to be 48 m/h and 30 minutes. And automatically entering the next step after the time is up.
i. And (4) secondary bubbling, namely bubbling with instrument gas to ensure that the resin is fully contacted with pure water. The instrument gas enters from the bottom of the resin tower.
And controlling the gas flow rate of the instrument for bubbling to be 20 Nm/h for 12 minutes, and automatically entering the next step after the time.
j. And (4) secondary sedimentation, namely standing and settling the resin layer boiled due to bubbling.
The standing time is 12 minutes, and the next step is automatically carried out after the standing time.
k. And (4) secondary drainage, namely discharging the washing wastewater in the resin tower by using instrument gas.
And controlling the gas flow of the instrument to be 20 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the waste water in the tower is drained, and automatically entering the next step.
In order to wash and discharge all the hydrochloric acid remaining in the resin, the steps of h washing, i bubbling, j settling and k draining were repeated once.
And l, alkali washing, namely diluting a sodium hydroxide solution with the mass concentration of 32% to a dilute sodium hydroxide solution with the mass concentration of about 4% by a mixer with pure water. The dilute sodium hydroxide solution is fed into the resin layer from the upper distribution pipe of the resin tower, and the weak base water is discharged from the bottom of the resin tower.
Controlling the flow rate of the sodium hydroxide solution with the mass concentration of 32% to be 3.8 m/h, controlling the flow rate of pure water to be 35.65 m/h, controlling the alkali washing time to be 90 min, and automatically entering the next step after the time comes.
And m, bubbling for three times, namely bubbling with instrument gas to ensure that the resin layer is in full contact reaction with alkali liquor, and the instrument gas enters from the bottom of the tower.
And controlling the gas flow rate of the instrument for bubbling to be 20 Nm/h for 12 minutes, and automatically entering the next step after the time.
And n, settling for three times, namely standing and settling the resin layer boiled due to bubbling.
The standing and settling time is 20 minutes, and the next step is automatically carried out after the time is up.
And o, discharging alkali water, namely discharging the dilute alkali water in the resin tower by using instrument gas.
And controlling the gas flow of the instrument to be 20 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the waste water in the tower is drained, and automatically entering the next step.
And p, secondary water washing, namely washing the residual caustic soda solution in the resin tower by using pure water. Pure water enters from the upper distribution pipe of the resin tower, and waste water is discharged from the bottom of the tower.
Controlling the flow of pure water for washing to be 48 m/h, and the time to be 20 minutes, and automatically entering the next step after the time.
And q, bubbling for four times, namely bubbling with instrument gas to ensure that the resin is fully contacted with pure water, wherein the instrument gas enters from the bottom of the resin tower.
And controlling the gas flow rate of the instrument for bubbling to be 20 Nm/h for 12 minutes, and automatically entering the next step after the time.
And r, four times of sedimentation, namely standing and settling the resin layer boiled due to bubbling.
The settling time was 10 minutes and the next step was automatically carried out by time.
s. tertiary drainage: and discharging the weak alkaline water in the resin tower by instrument gas.
And controlling the gas flow of the instrument to be 20 Nm/h, and triggering a liquid level switch at the bottom of the resin tower after the waste water in the tower is drained, and automatically entering the next step.
And t, filling salt water, namely enabling refined salt water to enter and fill the resin tower. The salt water enters from the bottom of the resin tower, and the waste water is discharged from the top of the resin tower.
And (3) filling the resin tower with qualified refined brine processed by the resin tower, and controlling the brine flow to be 34 m/h and the time to be 90 minutes.
The regeneration of the resin tower is completed.
Adopt traditional resin tower regeneration mode, carry out once regeneration to the resin tower, it is 14.37m to need 18% (mass concentration) hydrochloric acid to consume to carry out the high-yield cultivation, 32% (mass concentration) caustic soda consumes to carry out the high-yield cultivation for 6.84 m, and pure water consumes to carry out the high-yield cultivation for 335 m, produces waste water 455.97 m. The regeneration method provided by the invention is used for regenerating the resin tower once, and under the premise of ensuring good regeneration effect of the resin tower, the 18% hydrochloric acid consumption is 14.37m for thin film rice fruit year, the 32% caustic soda consumption is 5.7 m for thin film rice fruit year, the pure water consumption is 175 m for thin film rice fruit year, and the wastewater produced by thin film rice fruit year 242.17 m for thin film rice fruit year. The consumption of 32% caustic soda is reduced by 16.7%, the consumption of pure water is reduced by 47.8%, and the amount of generated wastewater is reduced by 46.9%.
Unless otherwise specified, the proportions in the present invention are mass proportions, and the percentages are mass percentages.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art will understand that various changes, modifications and substitutions can be made without departing from the spirit and scope of the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A chelate resin regeneration process in a secondary brine refining process is characterized in that: the method comprises the following process steps: draining, bubbling and settling.
2. The process of claim 1, wherein the regeneration of the chelating resin is carried out by the following steps: also comprises the following process steps: draining saline water, backwashing, acid washing, waste acid liquor drainage, water washing and alkali washing.
3. The process of claim 1, wherein the regeneration of the chelating resin is carried out by the following steps: the following steps are carried out in sequence: draining saline water, backwashing, primary draining, primary acid washing, primary bubbling, primary settling, draining waste acid liquor, primary washing, secondary bubbling, secondary settling, secondary draining, alkali washing, tertiary bubbling, tertiary settling, draining alkaline water, secondary washing, quaternary bubbling, quaternary settling, tertiary draining and filling saline water.
4. The process of claim 3, wherein the regeneration of the chelating resin is carried out by the following steps: the primary bubbling: controlling the flow rate of the instrument gas for bubbling to be 18-22 Nm/h, and the time to be 10-15 minutes.
5. The process of claim 3, wherein the regeneration of the chelating resin is carried out by the following steps: the primary sedimentation time is 100-150 minutes.
6. The process of claim 3, wherein the regeneration of the chelating resin is carried out by the following steps: and performing primary water washing, wherein the flow rate of pure water for water washing is controlled to be 45-50m and the time is 20-40 minutes.
7. The process of claim 3, wherein the regeneration of the chelating resin is carried out by the following steps: and (3) backwashing: controlling the backwashing pure water flow rate to be 50-70 m/h, and controlling the backwashing time to be 25-40 min.
8. The process of claim 3, wherein the regeneration of the chelating resin is carried out by the following steps: and in the primary pickling, the hydrochloric acid flow is 14-15m, the pure water flow is 24-25 m, and the pickling time is 50-70 minutes.
9. The process of claim 3, wherein the regeneration of the chelating resin is carried out by the following steps: and (3) carrying out alkaline washing, wherein the flow of the sodium hydroxide solution is 3-4 m/h, the flow of pure water is 35-36 m/h, and the alkaline washing time is 80-100 minutes.
10. The process of claim 3, wherein the regeneration of the chelating resin is carried out by the following steps: and (4) filling with brine, wherein the brine flow is controlled to be 30-40m for carrying out the year/h, and the time is 80-100 minutes.
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| CN202011150818.3A CN112295610A (en) | 2020-10-24 | 2020-10-24 | Chelate resin regeneration process in secondary brine refining process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113461098A (en) * | 2021-06-30 | 2021-10-01 | 钱中明 | Regeneration equipment and process for adsorbing heavy metal in water by using complexing resin |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0483592A (en) * | 1990-07-26 | 1992-03-17 | Mitsubishi Heavy Ind Ltd | Treatment of waste chemical washing solution |
| CN102923661A (en) * | 2012-11-29 | 2013-02-13 | 昊华宇航化工有限责任公司 | Anolyte clarifying tank waste chlorine gas recovery technology in ionic membrane caustic soda production |
| CN104624250A (en) * | 2014-12-25 | 2015-05-20 | 新疆中泰化学股份有限公司 | Chelate resin tower regeneration method |
| CN105002519A (en) * | 2014-04-22 | 2015-10-28 | 蓝星(北京)化工机械有限公司 | Secondary brine refining method for making large scale chelating resin tower achieve water saving effect |
| CN207628433U (en) * | 2017-12-12 | 2018-07-20 | 焦作煤业（集团）开元化工有限责任公司 | Backwash resin tower is exempted from a kind of resin regeneration |
| CN110203992A (en) * | 2019-05-24 | 2019-09-06 | 重庆市映天辉氯碱化工有限公司 | A method of reducing chelate resin tower regenerative wastewater discharge amount |
-
2020
- 2020-10-24 CN CN202011150818.3A patent/CN112295610A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0483592A (en) * | 1990-07-26 | 1992-03-17 | Mitsubishi Heavy Ind Ltd | Treatment of waste chemical washing solution |
| CN102923661A (en) * | 2012-11-29 | 2013-02-13 | 昊华宇航化工有限责任公司 | Anolyte clarifying tank waste chlorine gas recovery technology in ionic membrane caustic soda production |
| CN105002519A (en) * | 2014-04-22 | 2015-10-28 | 蓝星(北京)化工机械有限公司 | Secondary brine refining method for making large scale chelating resin tower achieve water saving effect |
| CN104624250A (en) * | 2014-12-25 | 2015-05-20 | 新疆中泰化学股份有限公司 | Chelate resin tower regeneration method |
| CN207628433U (en) * | 2017-12-12 | 2018-07-20 | 焦作煤业（集团）开元化工有限责任公司 | Backwash resin tower is exempted from a kind of resin regeneration |
| CN110203992A (en) * | 2019-05-24 | 2019-09-06 | 重庆市映天辉氯碱化工有限公司 | A method of reducing chelate resin tower regenerative wastewater discharge amount |
Non-Patent Citations (2)
| Title |
|---|
| 李娜等: ""螯合树脂塔再生操作优化"", 《氯碱工业》 * |
| 邵国斌，刘俊岐，付汉卿，张谦华主编: "《烧碱及聚氯乙烯树脂生产》", 30 September 2013, 郑州：黄河水利出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113461098A (en) * | 2021-06-30 | 2021-10-01 | 钱中明 | Regeneration equipment and process for adsorbing heavy metal in water by using complexing resin |
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