CN114849794B - Online recovery method of cationic resin - Google Patents
Online recovery method of cationic resin Download PDFInfo
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- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract
The invention provides an online recovery method of cationic resin, and belongs to the technical field of water softening treatment. Under the alkaline environment of the alkaline substance in the agent A, the surface active oil removal effect of the surfactant is enhanced, and suspended matters and greasy dirt colloid substances among the pores of the cationic resin can be removed in the backwashing process; in the salt feeding process, the inorganic acid in the agent B and CaCO generated on the surface of the cationic resin 3 Scale reaction for scale removal, capable of being combined with Fe 3+ Complex-forming salts with resin adsorbed Fe during operation 3+ The reaction achieves the effects of descaling, deironing and regeneration, and meanwhile, the corrosion inhibitor in the agent B can reduce the corrosion of the agent B to equipment such as a tank body, a pipeline, a valve and the like in the system. The invention stops recovering the resin exchange capacity by manually taking out the resin from the outside of the tank and using the equipment for cleaning every month, and thoroughly solves the problems of incomplete resin cleaning, time and labor waste and difficult guarantee of the exchange capacity after cleaning.
Description
Technical Field
The invention relates to the technical field of water softening treatment, in particular to an on-line recovery method of cationic resin.
Background
The softening and regenerating processes of most resin softening systems at present are as follows:
(1) backwashing: backwashing for 30min after the running period is finished;
(2) salt feedingThe link is as follows: after the backwashing is finished, the industrial salt solution is added to regenerate the resin for 2 hours until the density of the solution at the outlet of the resin tank is about 1.13g/cm 3 ；
(3) And (3) replacement link: replacing the industrial salt solution in the tank with clear water for 2h;
(4) primary forward washing: compacting the resin in the first-stage resin tank by using clear water in an up-in and down-out mode;
(5) and (3) secondary forward washing: and compacting the resin in the secondary resin tank by using clear water in an up-in and down-out mode.
The most common contamination encountered by cationic resins in oilfield wastewater purification water softening systems is the contamination of the resins with oil stains and the poisoning contamination with metal ions. Because of the adsorption effect of the resin, oil, suspended matters or metal ions in the water form a layer of covering layer on the surface of the resin, the resin with serious pollution cannot achieve the effect of complete cleaning by the cleaning force of the backwashing stage in the system, and the effective contact between the ions in the water and the resin is prevented, so that the exchange capacity is reduced, and the regeneration frequency of the resin is increased.
At present, a thick oil field boiler recycling sewage softening system aims at the resin which is seriously polluted, is not thoroughly backwashed in the system and has the exchange capacity which does not meet the requirement, most of the resin is selected to be drawn out of a resin tank, and the polluted resin is cleaned manually by means of some cleaning equipment. The main problems of this cleaning method are:
(1) time and labor are wasted, and a large amount of manpower is required to consume a large amount of time for cleaning;
(2) the efficiency is low, and the cleaning speed and the cleaning amount are low in the same time due to the limitation of manpower;
(3) the cost is higher, and the time cost and the economic cost are higher because the manual cleaning process is more complicated.
Disclosure of Invention
The invention aims to provide an on-line recovery method of cationic resin, which thoroughly solves the problems that resin cleaning is not thorough, time and labor are wasted, and the exchange capacity is difficult to ensure after cleaning.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides an online recovery method of cationic resin, which comprises the following steps: introducing clear water into a resin tank containing cationic resin by adopting a backwashing flow of a resin softening system, backwashing the cationic resin, introducing an agent A to continue backwashing when the backwashing is carried out until the effluent SS is less than 5mg/L, stopping backwashing when the pH value of the backwash is less than 0.5 and the pH value of the agent A, introducing an agent B into the resin tank by adopting the existing salt inlet flow in the resin softening system, and replacing aqueous solution in the resin tank by clear water when the pH value of the inlet water is less than 0.5 and the pH value of the agent B, and carrying out forward washing;
the agent A is an aqueous solution of a surfactant and an alkaline substance; the B agent can be mixed with Fe 3+ A salt of the complex, citric acid, hydrochloric acid and an aqueous solution of the corrosion inhibitor.
Preferably, the surfactant is one or more of sulfonate type, hydroxy/carboxylate type, sulfate type and phosphate type.
Preferably, the alkaline substance includes one or more of sodium hydroxide, potassium hydroxide, sodium carbonate and potassium carbonate.
Preferably, the catalyst is capable of reacting with Fe 3+ The complex forming salts include one or more of potassium fluoride, potassium thiocyanate, ammonium fluoride and ammonium bifluoride.
Preferably, the mass content of the surfactant in the agent A is 1-3%, and the mass content of the alkaline substance is 0.5-1%.
Preferably, the mass content of citric acid in the agent B is preferably 3-5%, the mass content of hydrochloric acid is preferably 2-4%, and the agent B can be mixed with Fe 3+ The mass content of the salt forming the complex is 5-10%, and the mass content of the corrosion inhibitor is 0.5-1%.
Preferably, the flow rate of the clean water is more than or equal to 8m/h; the flow rate of the agent A is less than or equal to 5m/h.
Preferably, the flow rate of the agent B is less than or equal to 5m/h. .
Under the alkaline environment of the alkaline substance in the agent A, the surface active oil removal effect of the surfactant is enhanced, and suspended matters and greasy dirt colloid substances among the pores of the cationic resin can be removed in the backwashing process;in the salt feeding process, citric acid and hydrochloric acid in the agent B and CaCO generated on the surface of the cationic resin 3 Scale reaction for scale removal, capable of being combined with Fe 3+ Complex-forming salts with resin adsorbed Fe during operation 3+ The reaction achieves the effects of descaling, deironing and regeneration, and meanwhile, the corrosion inhibitor in the agent B can reduce the corrosion of the agent B to equipment such as a tank body, a pipeline, a valve and the like in the system.
The resuscitation agent can be matched with an on-site resin tank and a softening system to stop recovery of the resin exchange capacity by manually taking out the resin from the tank and cleaning the resin by using equipment every month.
The results of the examples show that the resuscitating agent is matched with the existing softening system to clean the resuscitated resin, the resuscitating rate of the resin is increased from 55.85% to 91.34% after being regenerated by the traditional regeneration method, the standard requirement of the resuscitating rate of the resin is completely met, and the problems that the resin is not thoroughly cleaned, time and labor are wasted, and the exchange capacity is difficult to ensure after cleaning are thoroughly solved.
Detailed Description
The invention provides an online recovery method of cationic resin, which comprises the following steps: introducing clear water into a resin tank containing cationic resin by adopting a backwashing flow of a resin softening system, backwashing the cationic resin, introducing an agent A to continue backwashing when the backwashing is carried out until the effluent SS is less than 5mg/L, stopping backwashing when the pH value of the backwash is less than 0.5 and the pH value of the agent A, introducing an agent B into the resin tank by adopting the existing salt inlet flow in the resin softening system, and replacing aqueous solution in the resin tank by clear water when the pH value of the inlet water is less than 0.5 and the pH value of the agent B, and carrying out forward washing;
the agent A is an aqueous solution of a surfactant and an alkaline substance; the B agent can be mixed with Fe 3+ A salt of the complex, citric acid, hydrochloric acid and an aqueous solution of the corrosion inhibitor.
In the present invention, the raw materials used are commercially available products well known in the art, unless specifically described otherwise.
The following will explain the agent A.
In the invention, the agent A is an aqueous solution of a surfactant and an alkaline substance. In the present invention, the type of the surfactant is preferably one or more of a sulfonate type, a hydroxy/carboxylate type, a sulfate type, and a phosphate type, and the sulfonate type surfactant preferably includes sodium dodecylbenzenesulfonate, sodium sulfonate, sodium succinic diester sulfonate, or sodium hexadecyl succinic monoester sulfonate; the surfactant of the hydroxy/carboxylate salt preferably comprises oleoyl chloride sodium polyformal or laurinol carboxylate; the surfactant of the sulfate salt type preferably includes a sulfate salt of a secondary alkyl sulfate or a sulfate salt of an unsaturated alcohol; the surfactant of the phosphate salt type preferably includes an alkyl phosphate salt or a polymeric polyphosphate salt. In an embodiment of the invention, the surfactant is sodium dodecyl benzene sulfonate. The surfactant has the functions of cleaning and degreasing.
In the present invention, the alkaline substance preferably includes one or more of sodium hydroxide, potassium hydroxide, sodium carbonate and potassium carbonate, and when the alkaline substance is a plurality of the above substances, the present invention does not require any particular ratio of the alkaline substances. In the present invention, the alkaline substance functions to provide a suitable alkaline environment for the oil removal action of the surfactant.
In the present invention, the mass content of the surfactant in the agent A is preferably 1 to 3%, more preferably 1.5 to 2.5%; the mass content of the alkaline substance is preferably 0.5 to 1%, more preferably 0.7 to 0.8%.
In the present invention, the agent A is preferably obtained by dissolving a surfactant and an alkaline substance in water.
The following describes the agent B.
In the present invention, the agent B is capable of reacting with Fe 3+ A salt of the complex, citric acid, hydrochloric acid and an aqueous solution of the corrosion inhibitor.
In the present invention, the catalyst is capable of reacting with Fe 3+ The complex forming salt preferably comprises one or more of potassium fluoride, potassium thiocyanate, ammonium fluoride and ammonium bifluoride, more preferably potassium fluoride. In the present invention, the agent B can be mixed with Fe 3+ The mass content of the salt forming the complex is preferably 5 to 10%, more preferably 6 to 9%More preferably 7 to 8%. In the present invention, the above salt can be used in combination with Fe in a cationic resin 3+ Forming a complex, thereby removing Fe in the cationic resin 3+ 。
In the invention, the mass content of the citric acid in the agent B is preferably 3-5%, and the mass content of the hydrochloric acid is preferably 2-4%. In the present invention, citric acid and hydrochloric acid can be used in combination with CaCO in the resin 3 The scale reaction achieves the scale removal effect.
The invention has no special requirements on the specific type of the corrosion inhibitor, and all corrosion inhibitors known in the art can be used. In the embodiment of the invention, the corrosion inhibitor is an imidazoline general acidification corrosion inhibitor. In the present invention, the mass content of the corrosion inhibitor in the agent B is preferably 0.5 to 1%, more preferably 0.6 to 0.9%, and still more preferably 0.7 to 0.8%. In the invention, the corrosion inhibitor can reduce the corrosion of the agent B to equipment such as a tank body, a pipeline, a valve and the like in the system.
The invention has no special requirement on the preparation process of the agent B, and can directly react with Fe 3+ The salt forming the complex, citric acid, hydrochloric acid and corrosion inhibitor are dissolved in water.
An on-line resuscitation method of the cationic resin will be described below.
The invention adopts a resin softening system backwashing flow to introduce clear water into a resin tank containing cationic resin, the cationic resin is backwashed, and when the backwashing is carried out until the effluent SS is less than 5mg/L, the A agent is introduced to continue the backwashing.
The invention has no special requirement on the cation resin, and the cation resin which needs to be subjected to ion exchange for removing hardness can be used. In an embodiment of the invention, the cationic resin is contaminated cationic resin in a resin softening system of thick oil field boiler reuse water.
The present invention is not particularly limited to such resin softening systems, as are well known in the art.
In the invention, the flow rate of the clean water is preferably more than or equal to 8m/h, the invention firstly adopts clean water to carry out large-displacement backwashing, and suspended matters coated on the cationic resin are washed down in the backwashing process, so that the greasy dirt is exposed, and the cleaning effect of the agent A is fully exerted.
In the present invention, the flow rate of the agent A is preferably 5m/h or less. The present invention ensures that the agent A is sufficiently contacted with the resin by controlling the flow rate of the agent A within the above range.
According to the invention, the cleaning effect of the agent A is fully exerted by the disturbance to the resin in the large-displacement backwashing process, the resin layer loosens in the backwashing process, the resin achieves the maximum expansibility, meanwhile, the surface active oil removal effect of the surfactant is enhanced in the alkaline environment produced by the alkaline substances in the agent A, and suspended matters and greasy dirt colloid substances among pores of the cationic resin can be removed in the backwashing process.
When the pH value of the backwash water is different from that of the agent A by less than 0.5, the backwash is stopped, and the agent B is fed into the resin tank through the existing salt feeding flow in the resin softening system.
In the present invention, the flow rate of the agent B is preferably 5m/h or less.
In the liquid inlet flow, citric acid and hydrochloric acid in the agent B and CaCO generated on the surface of the cationic resin 3 Scale reaction for scale removal, capable of being combined with Fe 3+ Complex-forming salts with resin adsorbed Fe during operation 3+ The reaction achieves the effects of descaling, deironing and regeneration, and meanwhile, the corrosion inhibitor in the agent B can reduce the corrosion of the agent B to equipment such as a tank body, a pipeline, a valve and the like in the system.
In the invention, when the liquid inlet is carried out until the difference between the pH value of the water outlet and the pH value of the agent B is below 0.5, the liquid inlet flow is finished, and more preferably, the liquid inlet is stopped when the difference between the pH value of the water outlet and the pH value of the agent B is 0.3-0.5.
After the liquid inlet (agent B) process is finished, the invention uses clear water to replace the water solution in the resin tank for forward washing. The present invention has no special requirement on the replacement and forward washing process, and the replacement and forward washing processes well known in the art can be adopted.
The following describes the method of on-line resuscitation of cationic resins provided by the present invention in detail with reference to examples, but they should not be construed as limiting the scope of the invention.
Example 1
The boiler reuse water in the 1# thick oil treatment station of a certain oil field causes that cationic resin in a resin tank is wrapped by greasy dirt due to front-end water quality fluctuation, incomplete backwashing and the like, and calcium carbonate scale is generated on the surface of the resin due to water quality, so that the cationic resin is recovered online.
The specific resuscitation method is as follows:
introducing clean water into a resin tank containing cationic resin for backwashing, wherein the backwashing flow rate is 8m/h, introducing an agent A (the composition of the agent A is 1.5% sodium dodecyl benzene sulfonate plus 0.8% NaOH) for continuously backwashing when the backwashing flow rate is 8m/h and the effluent SS is less than 5mg/L, stopping backwashing when the pH value of the backwash until the effluent is different from the pH value of the agent A by 0.5, and then introducing an agent B (the composition of the agent B is 3m/h and the composition of 3% citric acid plus 3% HCl plus 8% potassium fluoride plus 0.8% corrosion inhibitor) into the resin tank through the existing salt inlet flow in a resin softening system, ending the liquid inlet when the pH value of the effluent is different from the pH value of the agent B by 0.3, and performing positive washing by using clean water to replace the aqueous solution in the resin tank.
Comparative example 1
The conventional backwash-salt feeding-replacement-forward washing process is adopted, and the difference from example 1 is that clear water backwash is adopted, and the salt feeding solution is an industrial sodium chloride salt solution with the mass fraction of 20%.
The result shows that after the resin resuscitation agent A and the resin resuscitation agent B are matched with a specific cleaning method, the recovery of the resin exchange capacity in a mode of manually taking the resin out of the tank and cleaning the resin by using equipment in each month is stopped, and the problems that the resin cleaning is not thorough, time and labor are wasted, and the exchange capacity is difficult to ensure after the cleaning are thoroughly solved. Meanwhile, the resin exchange capacity of the agent A and the agent B of the resuscitation agent is obviously increased; the specific results are shown in Table 1:
table 1 resin exchange Capacity measurements and comparative example 1 and recovery test data
| Treatment mode | Resin exchange Capacity, mmol/L | Resuscitation rate, percent |
| Novel resin | 4.565 | / |
| Comparative example 1 | 2.76 | 60.46 |
| Example 1 | 4.116 | 90.25 |
Example 2
The cationic resin in the softener group of the No. 6 heating station of a certain oil field is seriously polluted, the water production period is short, the replacement frequency is high, the comprehensive treatment cost of ton water is greatly increased, and the recovery is carried out on the cationic resin.
The specific resuscitation method is as follows:
introducing clean water into a resin tank containing cationic resin for backwashing, wherein the backwashing flow rate is 8m/h, introducing an agent A (the composition of the agent A is 1.5% sodium dodecyl benzene sulfonate plus 1% KOH) for continuously backwashing when the backwashing flow rate is 8m/h and the effluent SS is less than 5mg/L, stopping backwashing when the pH value of the effluent is different from the pH value of the agent A by 0.5, introducing an agent B (the composition of the agent B is 3.5% citric acid plus 2.5% HCl plus 6% potassium fluoride plus 0.8% corrosion inhibitor) into the resin tank through a salt inlet flow in a resin softening system, and finishing when the pH value of the effluent is different from the pH value of the agent B by 0.5, and after the liquid inlet flow is finished, replacing the aqueous solution in the resin tank with clean water for forward washing.
Comparative example 2
The conventional backwash-salt feeding-replacement-forward washing process is adopted, and the difference from example 2 is that clear water backwash is adopted, and the salt feeding solution is an industrial sodium chloride salt solution with the mass fraction of 20%.
The results of the example 2 and the comparative example 2 show that after the resin recovery agent A and the resin recovery agent B are matched with a specific cleaning method, the resin recovery rate is increased by at least 20 percent, and the problems that the resin cleaning is not thorough, time and labor are wasted and the exchange capacity is difficult to ensure after the cleaning are thoroughly solved. The specific results are shown in Table 2.
Table 2 resin exchange Capacity measurements and comparative example 2 and recovery of experimental data
| Treatment mode | Resin exchange Capacity, mmol/L | Resuscitation rate, percent |
| Novel resin | 4.565 | / |
| Comparative example 2 | 3.3 | 72.28 |
| Example 2 | 4.27 | 93.53 |
Example 3
The boiler reuse water in the 1# thick oil treatment station of a certain oil field causes that cationic resin in a resin tank is wrapped by greasy dirt due to front-end water quality fluctuation, incomplete backwashing and the like, and calcium carbonate scale is generated on the surface of the resin due to water quality, so that the cationic resin is recovered online.
The specific resuscitation method is as follows:
introducing clear water into a resin tank containing cationic resin for backwashing, wherein the backwashing flow rate is 8m/h, and introducing an agent A (the composition of the agent A is 1.7% of sodium dodecyl benzene sulfonate plus 1% K) when the backwashing flow rate is less than 5mg/L of effluent SS 2 CO 3 ) Continuing backwashing, wherein the flow speed of the agent A is 2.5m/h, and stopping backwashing when the pH value of the backwash water is different from the pH value of the agent A by 0.5, and feeding the agent B into the resin tank through the existing salt feeding flow in the resin softening system (the composition of the agent B is as follows: 3% citric acid, 3% HCl, 8% potassium fluoride and 0.8% corrosion inhibitor), wherein the flow rate of the liquid inlet is 3m/h when the agent B is fed, the liquid inlet is ended when the pH value of the liquid outlet is different from the pH value of the agent B by 0.5, and the water solution in the resin tank is replaced by clear water for forward washing. The resin recovery rate was 91.34%.
Example 4
The cationic resin in the softener group of the No. 6 heating station of a certain oil field is seriously polluted, the water production period is short, the replacement frequency is high, the comprehensive treatment cost of ton water is greatly increased, and the recovery is carried out on the cationic resin.
The specific resuscitation method is as follows:
introducing clear water into a resin tank containing cationic resin for backwashing, wherein the backwashing flow rate is 8m/h, introducing an agent A (the composition of the agent A is 1.5% sodium dodecyl benzene sulfonate plus 0.8% NaOH) for continuously backwashing when the backwashing flow rate is 8m/h and the effluent SS is less than 5mg/L, stopping backwashing when the pH value of the backwash until the effluent pH value is different from the pH value of the agent A by 0.5, introducing an agent B (the composition of the agent B is 3% citric acid plus 3% HCl plus 8% potassium fluoride plus 0.8% corrosion inhibitor) into the resin tank through a salt inlet flow in a resin softening system, wherein the flow rate of the inlet liquid is 3m/h, ending when the pH value of the outlet liquid is different from the pH value of the agent B by 0.3, and replacing the aqueous solution in the resin tank with clear water after the liquid inlet flow is completed, and performing forward washing. The resin recovery rate was 92.2%.
Comparative example 3
The traditional backwashing-salt feeding-replacement-forward washing process is adopted, and the difference from example 4 is that after the resin tank containing the cationic resin is backwashed by introducing clean water, firstly introducing 0.8% NaOH solution for backwashing for 20min, the backwashing flow rate is 3.5m/h, after the solution in the tank is replaced by the clean water, introducing 1.5% sodium dodecyl benzene sulfonate solution for backwashing for 20min, the flow rate is 3.5m/h, then introducing 3% citric acid+3% HCl+0.8% corrosion inhibitor solution into the resin tank through the salt feeding process, the flow rate is 3m/h, when the pH value of the effluent is different from the pH value of the B agent by 0.3, then introducing 8% potassium fluoride solution into the cationic resin tank for 20min, after the solution is replaced by the clean water, and forward washing is carried out.
The results of example 4 and comparative example 3 show that compared with the mode that the resin resuscitation agent A and B in the invention are matched with a specific cleaning method, the mode that the sodium dodecyl benzene sulfonate solution and the NaOH solution in the A agent and the citric acid+HCl+corrosion inhibitor solution and the potassium fluoride solution in the B agent are sequentially introduced into a cationic resin tank in batches has the defects of large wastewater amount, incomplete cleaning of the greasy dirt on the resin surface (the oil content of the effluent is measured to represent the cleaning effect of the greasy dirt on the resin surface when the A agent is introduced in example 4 and the oil content of the effluent is measured when the sodium dodecyl benzene sulfonate solution is introduced in comparative example 3), and the resin exchange capacity is low.
Table 3 comparative experimental data on the cleaning effect of the resin of example 4 and comparative example 3
The foregoing is merely a preferred embodiment of the present invention and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present invention, which are intended to be comprehended within the scope of the present invention.
Claims (5)
1. An on-line resuscitation method of cationic resin, characterized by comprising the following steps: introducing clear water into a resin tank containing cationic resin by adopting a backwashing flow of a resin softening system, backwashing the cationic resin, introducing an agent A to continue backwashing when the backwashing is carried out until the effluent SS is less than 5mg/L, stopping backwashing when the pH value of the backwash is less than 0.5 and the pH value of the agent A, introducing an agent B into the resin tank by adopting the existing salt inlet flow in the resin softening system, and replacing aqueous solution in the resin tank by clear water when the pH value of the inlet water is less than 0.5 and the pH value of the agent B, and carrying out forward washing;
the agent A is an aqueous solution of a surfactant and an alkaline substance; the B agent can be mixed with Fe 3+ Forming an aqueous solution of a salt of the complex, citric acid, hydrochloric acid and a corrosion inhibitor;
said compound being capable of reacting with Fe 3+ The complex forming salts include one or more of potassium fluoride, potassium thiocyanate, ammonium fluoride and ammonium bifluoride;
the mass content of the surfactant in the agent A is 1-3%, and the mass content of the alkaline substance is 0.5-1%;
the mass content of citric acid in the agent B is preferably 3-5%, the mass content of hydrochloric acid is preferably 2-4%, and the agent B can be mixed with Fe 3+ The mass content of the salt forming the complex is 5-10%, and the mass content of the corrosion inhibitor is 0.5-1%.
2. The on-line resuscitation method according to claim 1, wherein said surfactant is one or more of a sulfonate type, a hydroxy/carboxylate type, a sulfate type and a phosphate type.
3. The on-line resuscitation method according to claim 1, wherein said alkaline substance comprises one or more of sodium hydroxide, potassium hydroxide, sodium carbonate and potassium carbonate.
4. The online resuscitation method according to claim 1, wherein the flow rate of clean water during backwashing is not less than 8m/h; the flow rate of the agent A is less than or equal to 5m/h.
5. The on-line resuscitation method according to claim 1, wherein the flow rate of agent B is less than or equal to 5m/h.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002263506A (en) * | 2001-03-07 | 2002-09-17 | Santoku Kagaku Kogyo Kk | Method for preserving ion exchange resin packed column |
| CN112316989A (en) * | 2020-10-21 | 2021-02-05 | 华融化学股份有限公司 | Regeneration method of ion exchange resin |
| CN114345423A (en) * | 2022-01-21 | 2022-04-15 | 欧尚元(天津)有限公司 | Continuous ion-exchange resin resuscitation method and system |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002263506A (en) * | 2001-03-07 | 2002-09-17 | Santoku Kagaku Kogyo Kk | Method for preserving ion exchange resin packed column |
| CN112316989A (en) * | 2020-10-21 | 2021-02-05 | 华融化学股份有限公司 | Regeneration method of ion exchange resin |
| CN114345423A (en) * | 2022-01-21 | 2022-04-15 | 欧尚元(天津)有限公司 | Continuous ion-exchange resin resuscitation method and system |
Non-Patent Citations (1)
| Title |
|---|
| 阳离子交换树脂铁污染复苏技术与应用;李福梅等;中国管理科学文献;第912-915页 * |
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