CN203253201U - Multistage resin column device for removing metal ion impurities in aluminum chloride solution - Google Patents
Multistage resin column device for removing metal ion impurities in aluminum chloride solution Download PDFInfo
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- CN203253201U CN203253201U CN 201320245154 CN201320245154U CN203253201U CN 203253201 U CN203253201 U CN 203253201U CN 201320245154 CN201320245154 CN 201320245154 CN 201320245154 U CN201320245154 U CN 201320245154U CN 203253201 U CN203253201 U CN 203253201U
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Abstract
The utility model discloses a multistage resin column device for removing metal ion impurities in an aluminum chloride solution. The multistage resin column device comprises at least two stages of strong acidic cation exchange resin column groups and at least two stages of chelate resin column groups which are independent and connected in sequence, wherein each stage of the strong acidic cation exchange resin column groups and the chelate resin column groups comprises 1-4 parallel resin columns. The multistage column device is simple in structure and has a good impurity removal effect; the effective operation time of resin is remarkably prolonged, a large amount of time and reagents consumed in elution and regeneration processes are saved, and the production efficiency is greatly improved.
Description
Technical field
The utility model relates to for the device of removing the impurity metal ion that liquor alumini chloridi contains, is specifically related to remove the multistage resin column device of the impurity metal ion that contains in the liquor alumini chloridi.
Background technology
In the process of industrial production liquor alumini chloridi, when preparing alumina solution such as the flyash acid system, owing to the purity of powdered coal ash not and the reason such as equipment pollution, usually contain the impurity such as a certain amount of iron, calcium, magnesium in the liquor alumini chloridi that makes.When preparing the industrial products such as aluminium polychloride, aluminium chloride or crystal aluminum chloride with such liquor alumini chloridi, these impurity are easy to enter in the product, and product quality is produced very adverse influence, and wherein the impact of iron tramp is especially serious.Therefore, remove the iron, calcium, the magnesium addition that contain in the liquor alumini chloridi, iron tramp particularly, to produce highly purified liquor alumini chloridi, be very crucial for industrial products such as preparation aluminium polychloride (particularly low iron aluminium polychloride), aluminium chloride and crystal aluminum chlorides (particularly low iron crystal aluminum chloride).
Remove at present the method for the impurity such as iron in the liquor alumini chloridi, calcium, magnesium, the alkali impurity removal method that adopt more, namely in liquor alumini chloridi, add alkali, for example NaOH makes the contamination precipitations such as iron, calcium, magnesium out, and aluminium hydroxide is owing to be amphiprotic substance, can react with the highly basic of capacity, the meta-aluminate water soluble that generates is realized Separation of Solid and Liquid by means such as filtrations again, and gained liquid is produced refining liquor alumini chloridi as raw material.This method complex process, operation inconvenience, cost is higher, and owing to needed at first acid adding to carry out acid before adding the alkali removal of impurities to dissolve, with the alkali metal ions such as iron, calcium, magnesium in the abundant stripping raw material, so the content of the alkali metal ions such as iron, calcium, magnesium is higher in the aluminium chloride raw material, alkali consumption is just larger, more be not suitable for large-scale production, so in the actual production, the method there is certain requirement for the content of iron, calcium, magnesium etc. in the aluminium chloride raw material.For relatively high liquor alumini chloridis of foreign metal ion concentration such as iron, calcium, magnesium, still there is not suitable knot screen at present.
Therefore, need a kind of device for removing the impurity such as liquor alumini chloridi iron, calcium, magnesium.
The utility model content
The purpose of this utility model is to provide a kind of multistage resin column device for removing liquor alumini chloridi iron, calcium, magnesium addition ion.
The purpose of this utility model is achieved by the following technical solution:
A kind of multistage resin column device for removing the liquor alumini chloridi foreign ion, comprise the strongly acidic cation-exchange post group and the chelating resin post group that connect successively, wherein said cation exchange resin column group and chelating resin post group comprise at least two-stage independently of one another, every grade of resin column that comprises that the 1-4 platform is arranged side by side.
Preferably, described cation exchange resin column can load one or more in the D001 type that is selected from, 732 types, 742 types, 7020H type, 7120H type, JK008 type or the SPC-1 type resin; Described chelating resin post can load one or more in the D401 type that is selected from, D402 type, D403 type, the D405 type resin.
A kind of preferred embodiment in, first order cation exchange resin column group and first order chelating resin post group comprise that independently of one another 1-2 platform blade diameter length ratio arranged side by side is the resin column of 1.5-3:1, and second level cation exchange resin column group and second level chelating resin post group comprise that independently of one another 2-4 platform blade diameter length ratio arranged side by side is the resin column of 0.5-0.8:1.
Preferably, described cation exchange resin column group and chelating resin post group comprise at least three grades independently of one another, and final stage cation exchange resin column group and the final stage chelating resin post group resin column that to be respectively 1 blade diameter length ratio be 0.5-0.8:1.
Preferably, except the final stage resin column, the resin inventory of cation exchange resin column groups at different levels equates that the resin inventory of chelating resin post groups at different levels equates.
In another preferred embodiment, first order cation exchange resin column group and first order chelating resin post group comprise that independently of one another 2-4 platform blade diameter length ratio is the resin column of 0.5-0.8:1, and final stage cation exchange resin column group and final stage chelating resin post group comprise that independently of one another 1-2 platform blade diameter length ratio is the resin column of 0.5-0.8:1.
Preferably, described cation exchange resin column group and chelating resin post group are respectively two-stage, wherein the first order and second level cation exchange resin column group are respectively two D001 type cation exchange resin columns arranged side by side and a D001 type cation exchange resin column, the first order and second level chelating resin post group are respectively two D401 type chelating resin posts arranged side by side and a D401 type chelating resin post, and the blade diameter length ratio of each resin column is 0.5-0.8:1.
Preferably, described cation exchange resin column and chelating resin post are respectively two-stage, wherein the first order and second level cation exchange resin column are respectively 732 type cation exchange resin columns and two 732 type cation exchange resin columns arranged side by side, the first order and second level chelating resin post are respectively a D402 type chelating resin post and two D402 type chelating resin posts arranged side by side, and the blade diameter length ratio of first order cation exchange resin column and first order chelating resin post is 1.5-3:1, and the blade diameter length ratio of second level cation exchange resin column and second level chelating resin post is 0.5-0.8:1.
Compare with existing alkali impurity-removing method, apparatus structure of the present utility model is simple, good impurity removing effect, the iron content in the liquor alumini chloridi (in iron oxide) can easily be down to below the 0.2mg/L, and content of calcium and magnesium (respectively in calcium oxide, magnesia) is down to below the 0.1mg/L.In addition, when with the resin of equivalent feed liquid of the same race being processed, resin than manying the arrangement mode significant prolongation that a resin column connects successively, has been saved the wash-out of resin, plenty of time and the reagent that regenerative process consumes from the effective run time that uses inefficacy, has greatly improved production efficiency.
Description of drawings
Fig. 1 shows the arrangement mode according to the resin column of a kind of embodiment of the present utility model.
Fig. 2 shows the arrangement mode according to the resin column of another kind of embodiment of the present utility model.
Fig. 3 shows the arrangement mode according to the resin column of another embodiment of the utility model.
The specific embodiment
Below the utility model is described further, but therefore the utility model is not subject to any restriction.In the situation that does not depart from design of the present utility model and restricted portion, the utility model can have other distortion.
Below the specific embodiment of the present utility model is described.
The utility model provides a kind of device of removing the iron that contains in the liquor alumini chloridi, calcium, magnesium addition ion, comprise the strongly acidic cation-exchange post group and the chelating resin post group that connect successively, wherein said cation exchange resin column group and chelating resin post group comprise at least two-stage independently of one another, every grade of resin column that comprises that the 1-4 platform is arranged side by side.
Wherein, described cation exchange resin column can load existing any one or multiple strongly acidic cation-exchange, is preferably selected from one or more in D001 type, 732 types, 742 types, 7020H type, 7120H type, JK008 type or the SPC-1 type resin; Described chelating resin post can load existing any one or a few chelating resin, is preferably selected from D401 type, D402 type, D403 type, the D405 type resin one or more.
Cationic ion-exchange resin is mainly used in removing the iron ion in the liquor alumini chloridi, because the ion-exchange capacity of iron ion significantly is better than calcium, magnesium and aluminium ion, so cationic ion-exchange resin meeting preferential adsorption iron ion, the calcium in the solution, magnesium ion and aluminium ion then enter interior continuation of chelating resin post in downstream and process.Chelating resin mainly adsorbs bivalent cation, be calcium, magnesium ion, chelating resin is to Tricationic simultaneously, also has suction-operated such as iron ion, if a small amount of iron ion is arranged not by cationic exchange resin adsorption in the liquor alumini chloridi, can be adsorbed by the chelating resin in downstream, thus the quality that guarantees to make with extra care liquor alumini chloridi.Process by such device, the iron in the liquor alumini chloridi, calcium and magnesium addition ion are adsorbed by resin column substantially, thus the liquor alumini chloridi that obtains making with extra care.Every grade of quantity that comprises of sum of series that described cation exchange resin column group and chelating resin post group comprise separately can be determined according to the measurer body of iron, calcium, magnesium ion impurity in the liquor alumini chloridi.
Preferably, first order cation exchange resin column group and first order chelating resin post group comprise one or two pyknic resin columns arranged side by side, that loading amount is larger separately, and second level cation exchange resin column group and second level chelating resin post group comprise respectively two to four thin and tall type resin columns arranged side by side.According to actual needs, the third level and above cation exchange resin column group and chelating resin post group can also be set, every grade can comprise one to four thin and tall type resin column.
Such arrangement mode is particularly useful for the larger situation of feed velocity.Have characteristics during the resin treatment feed liquid, namely when processing the high concentration feed liquid, the utilization rate of resin is low, loses efficacy when resin can reach capacity far away in the adsorbance of ion; And when processing low concentration feed liquid, the utilization rate of resin is relatively high.In addition, when the flow velocity of feed liquid was very fast, resin was abundant not to the absorption of foreign ion; And the flow velocity of feed liquid is when slower, and resin is more abundant to the absorption meeting of foreign ion.When adopting above-mentioned arrangement mode, the pyknic resin column that the resin loading amount is large is suitable for accepting the large feed liquid of flow velocity, and is conducive to remedy the short problem of efficiency lost resin time that the foreign ion of high concentration causes, and can make feed liquid obtain as far as possible fully bulk processing.Through after the above-mentioned bulk processing, feed liquid is carried out fine processing by many thin and tall type resin columns of subordinate again.Because the concentration of foreign ion significantly reduces in the feed liquid at this moment, and the feed velocity of the unit amount of resin of every resin column of process is slack-off, thereby foreign ion can fully be adsorbed.Through two-stage cation exchange resin column group at least with after two-stage chelating resin post group is processed at least, the foreign ion of the overwhelming majority in the feed liquid can be adsorbed, and obtains highly purified refining liquor alumini chloridi.
When cation exchange resin column group and chelating resin post group comprise more than three grades independently of one another, final stage cation exchange resin column group and final stage chelating resin post group are a thin and tall type resin column independently of one another, it is mainly as the safety pole of index control, and is chaotic in order to prevent the system that causes efficiency lost resin to cause because of reasons such as material flows.
Preferably, except the final stage resin column, the resin inventory of cation exchange resin column groups at different levels equates that the resin inventory of chelating resin post groups at different levels equates.For example, if first order cation exchange resin column group is a pyknic resin column, the resin loading amount is A, and second level cation exchange resin column group comprises three thin and tall type resin columns, and the resin loading amount that then designs every thin and tall type resin column is A/3; The loading amount of chelating resin post groups at different levels also adopts this principle, but the resin inventory of every grade of chelating resin post not necessarily equates with the resin inventory of every grade of cation exchange resin column group, specifically should determine according to the measurer body of various foreign ions in the liquor alumini chloridi.
Preferably, first order cation exchange resin column group and first order chelating resin post group comprise the resin column of two to four thin and tall types separately, and final stage cation exchange resin column group and final stage chelating resin post group comprise respectively the resin column of one to two thin and tall type.
Such arrangement mode is particularly useful for the moderate situation of feed velocity.Can adopt the pyknic resin column to accept feed liquid this moment, and begin namely feed liquid to be shunted and fine processing from first order resin column.The resin column quantity that the sum of series of resin column is every grade is decided by the concrete condition of impurity ion content in the feed liquid.Final stage resin column group adopts the resin column of one to two thin and tall type as the safety pole of index control.
The blade diameter length ratio of pyknic resin column described herein is 1.5-3:1, and the blade diameter length ratio of described thin and tall type resin column is 0.5-0.8:1.The blade diameter length ratio of resin column refers to the diameter of resin column and the ratio of height.
Not only impurity-eliminating effect is good to adopt the resin column arrangement mode of device of the present utility model, and when with the resin of equivalent feed liquid of the same race being processed, the running time of resin (being that resin is from using the effective run time of inefficacy) is than manying the arrangement mode significant prolongation that a resin column connects successively, save plenty of time and reagent that resin elution, regenerative process consume, greatly improved production efficiency.
A kind of preferred embodiment in, described cation exchange resin column group and chelating resin post group comprise two-stage independently of one another, wherein the first order and second level cation exchange resin column group are respectively two D001 type cation exchange resin columns arranged side by side and a D001 type cation exchange resin column, the first order and second level chelating resin post group are respectively two D401 type chelating resin posts arranged side by side and a D401 type chelating resin post, and the blade diameter length ratio of each resin column is 0.5-0.8:1.
Identical with present embodiment with resin kind and loading amount, three D001 type cation exchange resin columns are compared with the arrangement mode that three D401 type chelating resin posts are connected successively, and the resin overall operation time of present embodiment is 4.5 times of prior art.
In another preferred embodiment, described cation exchange resin column and chelating resin post comprise two-stage independently of one another, wherein the first order and second level cation exchange resin column are respectively 732 type cation exchange resin columns and two 732 type cation exchange resin columns arranged side by side, the first order and second level chelating resin post are respectively a D402 type chelating resin post and two D402 type chelating resin posts arranged side by side, and the blade diameter length ratio of first order cation exchange resin column and first order chelating resin post is 1.5-3:1, and the blade diameter length ratio of second level cation exchange resin column and second level chelating resin post is 0.5-0.8:1.
Identical with present embodiment with resin kind and loading amount, three 732 type cation exchange resin columns are compared with the arrangement mode that three D402 type chelating resin posts are connected successively, and the resin overall operation time of present embodiment is 4.25 times of prior art.
Below in conjunction with specific embodiment the utility model is described further, but therefore the utility model is not subject to any restriction.In the situation that does not depart from design of the present utility model and restricted portion, the utility model can have other distortion.
Embodiment 1
To contain aluminium 95 grams per liters (in aluminium oxide), iron content 1.4 grams per liters (in iron oxide), calcic 1.7 grams per liters (in calcium oxide), the liquor alumini chloridi that contains magnesium 1.1 grams per liters (in magnesia), regulate pH value to 1.5 with hydrochloric acid solution, temperature is heated to 69 ℃, be pumped in as shown in Figure 1 the multistage resin column group with resistance to acid attack, wherein resin column 11, D001 type cationic ion-exchange resin is housed in 12 and 13, resin column 14, D401 type chelating resin is housed in 15 and 16, every interior resin loading amount of resin column is respectively 20ml, and the blade diameter length ratio of every resin column is 0.6:1.Liquor alumini chloridi adopts following current to cross the post method and processes, and the supplied materials flow velocity of liquor alumini chloridi is 40ml/ hour.
After removal of impurities was processed, the refining liquor alumini chloridi that obtains contained aluminium 93 grams per liters (in aluminium oxide) after measured, iron content 1.7 mg/litre (in iron oxide), and calcic 0.9 mg/litre (in calcium oxide) contains magnesium 0.82 mg/litre (in magnesia).But the resin system continuous effective of present embodiment operation 18 hours, and the resin in the above-mentioned resin column that conventional series system connects generally namely lost efficacy after 4 hours in operation, the resin overall operation time of the arrangement mode of present embodiment is 4.5 times of prior art.
After finishing except miscellaneous operation, described cationic ion-exchange resin and chelating resin are carried out respectively wash-out and regeneration processing, make it to recover adsorption capacity.Wash-out and regeneration are processed and are all adopted following current to cross the post method.Eluant, eluent adopts water, and consumption is 3 times of resin cumulative volume, 35 ℃ of eluting temperatures, flow velocity be 1 times of resin volume/hour; Adopting mass concentration during regeneration is 5% hydrochloric acid, and consumption is 3 times of resin cumulative volume, and temperature is room temperature, flow velocity be 3 times of resin volumes/hour.After adopting such wash-out and regeneration to process, the foreign ion in the resin can be reused for removal of impurities and process by wash-out.
Embodiment 2
To contain aluminium 85 grams per liters (in aluminium oxide), iron content 1.8 grams per liters (in iron oxide), calcic 1.3 grams per liters (in calcium oxide), the liquor alumini chloridi that contains magnesium 1.4 grams per liters (in magnesia), regulate pH value to 1.3 with hydrochloric acid solution, temperature is heated to 73 ℃, is pumped in as shown in Figure 2 the multistage resin column group with resistance to acid attack, wherein in the resin column 21,22 and 23 732 type cationic ion-exchange resins are housed, D402 type chelating resin is housed in the resin column 24,25 and 26. Resin column 21 and 24 blade diameter length ratio are 1.8:1, and the resin loading amount is respectively 40ml; Resin column 22,23,25 and 26 blade diameter length ratio are 0.6:1, and the resin loading amount is respectively 20ml.Liquor alumini chloridi adopts following current to cross the post method and processes, and the supplied materials flow velocity of liquor alumini chloridi is 60ml/ hour.
After removal of impurities is processed, obtain refined crystalline aluminium chloride liquid and contain aluminium 84.2 grams per liters (in aluminium oxide), iron content 1.7 mg/litre (in iron oxide), calcic 0.88 mg/litre (in calcium oxide) contains magnesium 0.84 mg/litre (in magnesia).But the resin system continuous effective of present embodiment operation 17 hours, and the resin in the above-mentioned resin column that conventional series system connects generally namely lost efficacy after 4 hours in operation, the resin overall operation time of the arrangement mode of present embodiment is 4.25 times of prior art.
After finishing except miscellaneous operation, described cationic ion-exchange resin and chelating resin are carried out respectively wash-out and regeneration processing, make it to recover adsorption capacity.Wash-out and regeneration are processed and are all adopted following current to cross the post method.It is 2% hydrochloric acid that eluant, eluent adopts mass concentration, and consumption is 2 times of resin cumulative volume, and eluting temperature is 45 ℃, flow velocity be 1 times of resin volume/hour, adopt altogether during wash-out; Adopting mass concentration during regeneration is 2% hydrochloric acid, and consumption equals the resin cumulative volume, and temperature is room temperature, flow velocity be 2 times of resin volumes/hour.After adopting such wash-out and regeneration to process, the foreign ion in the resin can be reused for removal of impurities and process by wash-out.
Embodiment 3
To contain aluminium 88 grams per liters (in aluminium oxide), iron content 2.7 grams per liters (in iron oxide), calcic 1.5 grams per liters (in calcium oxide), the liquor alumini chloridi that contains magnesium 1.2 grams per liters (in magnesia), regulate pH value to 1.3 with hydrochloric acid solution, temperature is heated to 73 ℃, be pumped in as shown in Figure 3 the multistage resin column group with resistance to acid attack, wherein in the resin column 31,32,33,34,35,36 and 37 7020H type cationic ion-exchange resin is housed, D403 type chelating resin is housed in the resin column 38,39 and 40. Resin column 31,32,33,34,35,36,37,39 and 40 blade diameter length ratio are 0.6:1, and the resin loading amount is respectively 20ml; The blade diameter length ratio of resin column 38 is 1.8:1, and the resin loading amount is 40ml;Liquor alumini chloridi adopts following current to cross the post method and processes, and the supplied materials flow velocity of liquor alumini chloridi is 60ml/ hour.
After removal of impurities is processed, obtain refined crystalline aluminium chloride liquid and contain aluminium 86.9 grams per liters (in aluminium oxide), iron content 1.69 mg/litre (in iron oxide), calcic 0.86 mg/litre (in calcium oxide) contains magnesium 0.83 mg/litre (in magnesia).But the resin system continuous effective of present embodiment operation 20 hours, and the resin in the above-mentioned resin column that conventional series system connects generally namely lost efficacy after 4 hours in operation, the resin overall operation time of the arrangement mode of present embodiment is 5 times of prior art.
After finishing except miscellaneous operation, described cationic ion-exchange resin and chelating resin are carried out respectively wash-out and regeneration processing, make it to recover adsorption capacity.Wash-out and regeneration are processed and are all adopted following current to cross the post method.It is 2% hydrochloric acid that eluant, eluent adopts mass concentration, and consumption is 2 times of resin cumulative volume, and eluting temperature is 45 ℃, flow velocity be 1 times of resin volume/hour, adopt altogether during wash-out; Adopting mass concentration during regeneration is 2% hydrochloric acid, and consumption equals the resin cumulative volume, and temperature is room temperature, flow velocity be 2 times of resin volumes/hour.After adopting such wash-out and regeneration to process, the foreign ion in the resin can be reused for removal of impurities and process by wash-out.
Claims (8)
1. multistage resin column device that is used for removing the liquor alumini chloridi impurity metal ion, it is characterized in that, described device comprises strongly acidic cation-exchange post group and the chelating resin post group that connects successively, wherein said cation exchange resin column group and chelating resin post group comprise at least two-stage independently of one another, every grade of resin column that comprises that the 1-4 platform is arranged side by side.
2. device according to claim 1 is characterized in that, the resin of described cation exchange resin column filling is selected from one or more in D001 type, 732 types, 742 types, 7020H type, 7120H type, JK008 type or the SPC-1 type; The resin of described chelating resin post filling is selected from one or more in D401 type, D402 type, D403 type, the D405 type.
3. device according to claim 1, it is characterized in that, first order cation exchange resin column group and first order chelating resin post group comprise that independently of one another 1-2 platform blade diameter length ratio arranged side by side is the resin column of 1.5-3:1, and second level cation exchange resin column group and second level chelating resin post group comprise that independently of one another 2-4 platform blade diameter length ratio arranged side by side is the resin column of 0.5-0.8:1.
4. device according to claim 3, it is characterized in that, described cation exchange resin column group and chelating resin post group comprise at least three grades independently of one another, and final stage cation exchange resin column group and the final stage chelating resin post group resin column that to be respectively 1 blade diameter length ratio be 0.5-0.8:1.
5. device according to claim 4 is characterized in that, except the final stage resin column, the resin inventory of cation exchange resin column groups at different levels equates that the resin inventory of chelating resin post groups at different levels equates.
6. device according to claim 1, it is characterized in that, first order cation exchange resin column group and first order chelating resin post group comprise that independently of one another 2-4 platform blade diameter length ratio is the resin column of 0.5-0.8:1, and final stage cation exchange resin column group and final stage chelating resin post group comprise that independently of one another 1-2 platform blade diameter length ratio is the resin column of 0.5-0.8:1.
7. device according to claim 1, it is characterized in that, described cation exchange resin column group and chelating resin post group are respectively two-stage, wherein the first order and second level cation exchange resin column group are respectively two D001 type cation exchange resin columns arranged side by side and a D001 type cation exchange resin column, the first order and second level chelating resin post group are respectively two D401 type chelating resin posts arranged side by side and a D401 type chelating resin post, and the blade diameter length ratio of each resin column is 0.5-0.8:1.
8. device according to claim 1, it is characterized in that, described cation exchange resin column group and chelating resin post group are respectively two-stage, wherein the first order and second level cation exchange resin column group are respectively 732 type cation exchange resin columns and two 732 type cation exchange resin columns arranged side by side, the first order and second level chelating resin post group are respectively a D402 type chelating resin post and two D402 type chelating resin posts arranged side by side, and the blade diameter length ratio of the chelating resin post of the cation exchange resin column of the first order and the first order is 1.5-3:1, and the blade diameter length ratio of the chelating resin post of the cation exchange resin column of the second level and the second level is 0.5-0.8:1.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105174556A (en) * | 2015-10-16 | 2015-12-23 | 南京大学 | High-acidity high-iron heavy metal wastewater quality-divided resource recycling method |
| WO2018125976A1 (en) * | 2016-12-29 | 2018-07-05 | Henkel Ag & Co. Kgaa | Electro-ceramic coating bath cleanup by a hybrid ion exchange precipitation process |
-
2013
- 2013-05-08 CN CN 201320245154 patent/CN203253201U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105174556A (en) * | 2015-10-16 | 2015-12-23 | 南京大学 | High-acidity high-iron heavy metal wastewater quality-divided resource recycling method |
| CN105174556B (en) * | 2015-10-16 | 2017-10-24 | 南京大学 | A kind of method of peracid high ferro heavy metal wastewater thereby sub-prime resource reclaim |
| WO2018125976A1 (en) * | 2016-12-29 | 2018-07-05 | Henkel Ag & Co. Kgaa | Electro-ceramic coating bath cleanup by a hybrid ion exchange precipitation process |
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