CN1011403B - Method for regeneration of ion exchanging resin by co2 - Google Patents
Method for regeneration of ion exchanging resin by co2Info
- Publication number
- CN1011403B CN1011403B CN89103379A CN89103379A CN1011403B CN 1011403 B CN1011403 B CN 1011403B CN 89103379 A CN89103379 A CN 89103379A CN 89103379 A CN89103379 A CN 89103379A CN 1011403 B CN1011403 B CN 1011403B
- Authority
- CN
- China
- Prior art keywords
- water
- resin
- exchange resin
- carbonic acid
- regeneration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000011347 resin Substances 0.000 title claims description 59
- 229920005989 resin Polymers 0.000 title claims description 59
- 230000008929 regeneration Effects 0.000 title claims description 28
- 238000011069 regeneration method Methods 0.000 title claims description 28
- 238000000034 method Methods 0.000 title claims description 17
- 238000005342 ion exchange Methods 0.000 title description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 66
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 34
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 11
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 11
- 230000001172 regenerating effect Effects 0.000 claims abstract description 8
- 235000011089 carbon dioxide Nutrition 0.000 claims description 19
- 238000002156 mixing Methods 0.000 claims description 17
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 7
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 6
- 230000007704 transition Effects 0.000 claims description 5
- 230000002378 acidificating effect Effects 0.000 claims description 3
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 claims description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 claims description 2
- 150000004649 carbonic acid derivatives Chemical class 0.000 claims description 2
- 239000000945 filler Substances 0.000 claims description 2
- 239000003729 cation exchange resin Substances 0.000 claims 2
- 238000010992 reflux Methods 0.000 claims 1
- 239000002253 acid Substances 0.000 abstract description 19
- 238000004519 manufacturing process Methods 0.000 abstract description 13
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 8
- 238000010612 desalination reaction Methods 0.000 abstract description 8
- 239000003513 alkali Substances 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 7
- 239000001569 carbon dioxide Substances 0.000 abstract description 7
- 239000000463 material Substances 0.000 abstract description 7
- 150000003839 salts Chemical class 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 6
- 239000000498 cooling water Substances 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 5
- 239000003795 chemical substances by application Substances 0.000 abstract description 3
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 3
- 239000003317 industrial substance Substances 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 3
- 229910000975 Carbon steel Inorganic materials 0.000 abstract description 2
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 239000003337 fertilizer Substances 0.000 abstract description 2
- 238000001179 sorption measurement Methods 0.000 abstract description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 abstract 1
- 235000013405 beer Nutrition 0.000 abstract 1
- 230000008569 process Effects 0.000 description 7
- 239000007788 liquid Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000010410 layer Substances 0.000 description 5
- 229910002651 NO3 Inorganic materials 0.000 description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 239000002585 base Substances 0.000 description 3
- 238000010828 elution Methods 0.000 description 3
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 239000011241 protective layer Substances 0.000 description 3
- DPEYHNFHDIXMNV-UHFFFAOYSA-N (9-amino-3-bicyclo[3.3.1]nonanyl)-(4-benzyl-5-methyl-1,4-diazepan-1-yl)methanone dihydrochloride Chemical compound Cl.Cl.CC1CCN(CCN1Cc1ccccc1)C(=O)C1CC2CCCC(C1)C2N DPEYHNFHDIXMNV-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005115 demineralization Methods 0.000 description 2
- 230000002328 demineralizing effect Effects 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 235000012204 lemonade/lime carbonate Nutrition 0.000 description 2
- 238000005649 metathesis reaction Methods 0.000 description 2
- 229920000915 polyvinyl chloride Polymers 0.000 description 2
- 239000004800 polyvinyl chloride Substances 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 230000002441 reversible effect Effects 0.000 description 2
- 241000212977 Andira Species 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- CERQOIWHTDAKMF-UHFFFAOYSA-N Methacrylic acid Chemical compound CC(=C)C(O)=O CERQOIWHTDAKMF-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 150000007516 brønsted-lowry acids Chemical class 0.000 description 1
- 150000007528 brønsted-lowry bases Chemical class 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000003020 moisturizing effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000009418 renovation Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 235000019600 saltiness Nutrition 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Images
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The present invention uses carbon dioxide as a regenerating agent for regenerating inactive ion exchange resin used for partial desalination or pre desalination; home-made ion exchange resin is used as an adsorption material, and standard components and plain carbon steel are used as equipment materials. The present invention has the advantages of simplicity, industrial chemicals of acid and alkali saving, low running cost and no environmental pollution; the present invention is suitable for large, medium and small sized fertilizer chemical enterprises to produce pentacyclic cooling water, beer brewing water production, and the pre desalination of the raw water with high carbonate hardness and strong acid salt. The technology of the present can also be used for the treatment of brackish water, and the heavy metal removal from wastewater.
Description
The invention belongs to feedwater or field of waste water treatment, relate in particular to ion-exchange demineralization renovation process and equipment.
The lower concentration salt is domestic in the removal water generally all adopts the traditional ion exchange process of strong type resin as sorbing material, water section or whole desalination is satisfied produced and life requirement.When the advantage of ion exchange technique is to keep in the water benefit materials, can removes influence life in the water effectively and drink all kinds of materials with production application.Resin can add regenerator after losing efficacy, and made it to return to original state.Resin almost can unrestrictedly be reused.Its shortcoming then shows, when regenerating positive resin with strong acid, and H only
+Ion works, OH only during with highly basic regeneration negative resin
-Ion plays replacement(metathesis)reaction, and all the other integral parts are not utilized in the regenerator, makes that saltiness has increased by one times in the regenerator.In addition, the strong type resin is very little to the avidity of proton and hydroxyl ion, need add the regenerator than the high 100-200% of stoichiometric quantity, just can make resin regeneration complete.So both consumed in a large number as the acid or the alkali of industrial chemicals, and caused the regenerator consumption costs to improve, the water surrounding salinization has aggravated the supply and demand tense situation of China chemical industry acid-base raw materials; Some Production in Chemical Plant process tail gas carbonic acid gas enters also contaminate environment of atmosphere simultaneously.
The external method of removing low dense salt in the water also is to adopt the conventional ion exchange process basically, with domestic the same, also is faced with the challenge of same problem and protection water resources.In order to reduce recovery regeneration of ion-exchange resin agent consumption, mainly use combination desalination from water of weak type resin or strong type and weak type resin in recent years.With the exception of this, also developed the Sul-bisul method, hot method of reproduction and brine electrolysis all are in the applied research stage at present as regenerator etc., are not put to as yet produce and implement.
West Germany adopts CARIX(carbonic acid gas regenerating ion exchange resin from the beginning in 1985) technology the exhausted resin that is used for regenerating from tap water removal part hardness and nitrate.The Processes and apparatus design all belongs to Deutsches Reichs-Patent.Select Amberlite IRC-50 and IRA 458 resins ion-exchange filter for use by 5: 6 volumetric ratio uniform mixing compositions, with 7 meters/time flow velocity system water, maximum water production rate 44 bed volumes, original water hardness is reduced to 5.4 equivalent parts per millions by 10.8 equivalent parts per millions, and nitrate reduces to 25 mg/litre by 40 mg/litre.Counter-current operation is adopted in regeneration, and carbonic acid gas is at 6kg/cm
2Be dissolved under the pressure and be prepared into regenerated liquid in the former water and be stored in 60 meters
3In the container with 2.5 meters/time flow velocity turbulent flow regeneration 3 hours.Unit volume resin elution hardness amount is 237.6 equivalent parts per millions.Have three shortcomings in the CARIX Production Flow Chart: (1) has adopted expensive methacrylic acid type resin; (2) the turbulent flow mode is regenerated and has been destroyed the protective layer of resin, and the resin breakage rate is big; (3) the regenerated liquid storage vessel is excessive need use high pressure resistant stainless steel; (4) be confined to handle domestic water.
The object of the present invention is to provide a kind of technology of carbonic acid gas regeneration inefficacy ion exchange resin of improvement, and that this ion exchange resin is used for from water is partially desalted or give desalination.Adopt homemade ion exchange resin as sorbing material, domestic standard parts and plain carbon stool be as equipment and materials, has simplely, and less investment is saved industrial chemicals bronsted lowry acids and bases bronsted lowry, advantage that working cost is low, free from environmental pollution.Ion exchange resin described in this processing method is to be applied to recirculated cooling water, is particularly useful for having the factory and enterprise in carbonic acid gas source, large, medium and small type chemical industry of chemical fertilizer enterprise, production cycle water coolant; Brewage water etc., and contain high carbon acid carbonate hardness and high strong acid salt former water give desalting treatment.This ion exchange resin also can be applicable to the processing of brackish water and remove heavy metal from waste water, and resin was used CO after losing efficacy
2Regenerate.
Principal character of the present invention is to the improvement with carbonic acid gas regenerating ion exchange resin technology.And above two kinds of resins are used for desalination, removing heavy metals from water, waste water.Adopt cheap acrylic type weakly acidic cationic exchanger resin, vinylbenzene highly basic I type anionite-exchange resin respectively from water the part hard-off remove alkali and remove strong acid salt, or the hybrid resin that adopts vinylbenzene highly basic I type anionite-exchange resin and acrylic type weak acid sun to make up from exchange resin, the part hard-off is removed alkali and is removed strong acid salt from water.With carbonic acid gas and water through the two-stage mixing tank.One-level is that the Venturi-type steam injector mixes with water, and the secondary mixing tank adopts to fill has the pressure-pot that increases air-water blended filler, makes carbonic acid gas and water in 5～6 kilograms per centimeter
2The thorough mixing dissolving reaches capacity under the pressure, and prepared carbonic acid soln is regenerated to exhausted resin, and regeneration adopts the transition flow operation that resin layer is kept relative stability, not random layer.
The inventive method is the reversible equilibrium principle according to ion-exchange, utilizes the carbonic acid ionization product H of the carbonic acid gas formation that is dissolved in the water under certain pressure
+With HCO
- 3The ionic replacement(metathesis)reaction makes resin return to original state.
Technical scheme of the present invention is as follows: utilize single of weak acid positive resin, single of strong base negative resin and mix bed by weak acid highly basic by the ion-exchange of 1: 1 volumetric ratio combination and under selected optimum flow rate, make water, water quality meets recirculated cooling water moisturizing and the requirement of brewage water, incorporates the water of productive use system into.After resin is exhausted control fails point, the carbonic acid gas that utilization is dissolved in the water under certain pressure is after the dissolving of secondary mixing tank thorough mixing reaches capacity, regenerate in the transition flow mode with selected optimum flow rate again, make resin return to original state, resin bed drops into the system water cycle after backwash.Regeneration waste liquid directly enters water body by the outfall sewer net.
Description of drawings: accompanying drawing is ion-exchange demineralization carbonic acid gas regeneration production equipment schema
[1], [2], [3] water-in and water-out valve, [4] boosting pump, [5], [6], [7] Venturi injector mixer, [8] mixing tank, [9] ion-exchanger.
The advantage that the present invention has is:
The present invention replaces expensive import metering system acid type Amber-Lite IRC-50 and IRA-458 resin with cheap acrylic type Lewatit CNP-80 and domestic D113 with 201 * 7 styrene highly basic I types and D251 resin, applies at home for this invention technology and paves Road.
By requirement of the present invention, (pressure is 6 kilograms per centimeter to carbon dioxide in the regenerative process2) with after former water is mixed with regenerative agent system and mixes by venturi one-level blender again in the abundant mixed dissolution of the secondary mixer that is filled with the polyvinyl chloride hollow ball reaches capacity replacement CARIX device the one-level blending tank make the carbon dioxide dissolving that reaches capacity by pumping circulation, its advantage is to adopt domestic standard parts and ordinary carbon steel tank to make the air-water mixer. Small investment, power consumption is low.
By method of the present invention; during regeneration with 5.6 meters/time flow velocity; keeping resin bed to be in the turbulent flow that replaces in the CARIX flow process with the transition flow regeneration under the metastable state regenerates; thereby make each water processed in the cycle resin maintain the protective layer of certain altitude; product water water quality than the regeneration of turbulent flow under identical pressure carbon dioxide condition improves, and unit volume absorption hardness amount can reach 328.6 equivalent parts per millions and exceed nearly 35% than CARIX technology unit volume resin adsorption hardness amount 237.6 equivalent parts per millions.
The invention has the advantages that the waste liquid that produces in the regenerative process need not add acid or/and alkali neutralization can directly enter water body, does not increase the salt load in waters, in having saved simultaneously and equalizing tank, acid or/and alkali storage tank and corresponding carrier vehicle.
The present invention be advantageous in that, good operation safety, production process is very little to equipment corrosion, has removed the labour protection measures and the special anticorrosive measure that prevent the soda acid burning accident from.
Embodiment 1
Recirculated cooling water desalination regeneration production equipment: form interchanger diameter phi 1500, cylindrical shell height H 4000,1.76 meters of cross-sectional areas by an interchanger, a carbon dioxide mix jar, 3 water-jet mixing tanks, a former water boosting pump
2, 3 meters of interior dress Lewatit CNP-80 weak acid positive resins
3, bed height is 1.7 meters.Filling polyvinyl chloride hollow ball increases the air water mixture length in the mixing tank, and carbonic acid gas is not established basin, directly quotes from pipe network.Former water boosts by water pump and sends into ion-exchanger in the system water process, with 11 meters/time economic velocity by resinbed, original water hardness is reduced to 2.5 equivalent parts per millions (50%) by 5.0 equivalent parts per millions; Basicity reduces to 1.29 equivalent parts per millions (68%) by 4.0 equivalent parts per millions, and maximum water production rate 100 bed volumes produce water and incorporate the recirculated cooling water water charging system into.During regeneration, the pressure that draws from pipe network is 6 kilograms per centimeter
2Carbon dioxide tentatively mix by Venturi one-level mixing tank; reach capacity through the further mixed dissolution of secondary mixing tank again, with 5.6 meters/time flow velocity, transition flow regeneration under resin layer keeps relative stability state; make the resin protective layer of keeping certain height, improve system water water quality.
Unit volume resin elution hardness amount reaches 321 equivalent parts per millions, and regeneration waste liquid directly enters water body, need not add the alkali neutralization.
Embodiment 2
Remove hardness and basicity in the water with homemade acrylic type D113 weak acid resin, regenerate after the inefficacy.
The ion exchange column specification is φ 114 * H1200, fill 3 liters of D113 resins, the resin layer height is 82.6 millimeters, 7 ± 0.2 meters of water flow velocities of system/time, former total hardness of water reduces a nearly half by 6.6 equivalent parts per millions, maximum water production rate reaches 100 bed volumes, when equal hardness 3.7 equivalent parts per millions of level, basicity 1.3 equivalent parts per millions, system water process hardness removes 45.5%, basicity removes 78%, during regeneration, and pressure 5.2 kilograms per centimeter
2Carbonic acid gas through the air-water mixing tank mix reach capacity the back with 3.2 meters/time flow velocity maintenance resin layer relatively stable counter-current regeneration, unit resin elution hardness amount is 287.5 equivalent parts per millions.Regeneration waste liquid directly enters water drain.
Embodiment 3
Remove strong acid anion in the water with homemade D251 highly basic I type anionite-exchange resin, regenerate after the inefficacy.
According to the reversible equilibrium principle of ion-exchange as can be known, need add an amount of lime carbonate during separately with carbonic acid gas regeneration negative resin and come the strong acid that generates in the neutralization reaction process, improve the regeneration efficiency of negative resin.During regeneration, be that to feed pressure in 0.15% the calcium carbonate soln be 2 kilograms per centimeter to the concentration for preparing
2Carbon dioxide to saturated, with 3.2 meters/time flow velocity counter-current regeneration 0.5 liter of D251 resin losing efficacy, 3 hours, after backwash, drop into the system water running, can remove Cl when water production rate is 60 bed volumes
-Ion 42.46%, SO
2- 4Ion 91.80%, and NO
- 347.56%.The lime carbonate dosage is lower for good than Theoretical Calculation amount to get, and helps making full use of effective exchange capacity of resin.
Embodiment 4
The mixed bed of ion-exchange part from the brewage water of forming at 1: 1 by volumetric ratio with homemade D113 weak acid resin and 201 * 7 vinylbenzene highly basic I type negative resins removes hardness and nitrate, regenerates after the inefficacy.7.2 meters of water flow velocities of system/time, when maximum water production rate reached 100 bed volumes, hardness on average removed 35.7%, nitrate removal 35.9%, sulfate removal 70.1%.Exhausted resin is with 5.5 kilograms per centimeter
2The unsaturated carbonate solution that the water-soluble back of the carbonic acid gas of pressure forms carries out counter-current regeneration, drops into the system water running after just washing.
Claims (2)
1, a kind of method with the carbonic acid gas regenerating ion exchange resin, be to use the unsaturated carbonate solution of the water-soluble generation of carbonic acid gas to Lewatit CNP-80 or homemade acrylic type D113 weakly acidic cation-exchange resin after losing efficacy, vinylbenzene highly basic I type anionite-exchange resin, the hybrid resin that LewatitCNP-80 or homemade acrylic type D113 weakly acidic cation-exchange resin and vinylbenzene highly basic I type anionite-exchange resin are formed by volume at 1: 1 is regenerated, it is characterized in that, mix through the two-stage mixing tank with water with carbonic acid gas, one-level is mixed for the Venturi-type steam injector, secondary mixes employing and is filled with the pressure-pot mixing tank mixing that increases the air-water mixed fillers, the dissolving of carbonic acid gas and water thorough mixing is reached capacity, prepared carbonic acid soln is regenerated to above-mentioned exhausted resin, and regeneration adopts the not disorderly transition flow of the layer operation that resin layer is kept relative stability.
2, method according to claim 1 is characterized in that said regeneration is to adopt the reflux type operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN89103379A CN1011403B (en) | 1989-05-25 | 1989-05-25 | Method for regeneration of ion exchanging resin by co2 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN89103379A CN1011403B (en) | 1989-05-25 | 1989-05-25 | Method for regeneration of ion exchanging resin by co2 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1039569A CN1039569A (en) | 1990-02-14 |
| CN1011403B true CN1011403B (en) | 1991-01-30 |
Family
ID=4855095
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN89103379A Expired CN1011403B (en) | 1989-05-25 | 1989-05-25 | Method for regeneration of ion exchanging resin by co2 |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1011403B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8617398B2 (en) | 1996-08-12 | 2013-12-31 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| US8758720B2 (en) | 1996-08-12 | 2014-06-24 | Debasish Mukhopadhyay | High purity water produced by reverse osmosis |
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| CN100343665C (en) * | 2005-10-31 | 2007-10-17 | 上海轻工业研究所有限公司 | Method for determining ion exchange resin saturating point |
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| CN115364629B (en) * | 2022-09-13 | 2023-06-23 | 华能沁北发电有限责任公司 | System and method for comprehensively utilizing tail gas of thermal power plant in carbon reduction |
| CN115353249B (en) * | 2022-10-20 | 2023-02-03 | 山东金泽水业科技有限公司 | Wastewater treatment process for recovering high-purity sodium bicarbonate by carbon dioxide solidification |
| CN117548155B (en) * | 2024-01-11 | 2024-03-29 | 山东省水利科学研究院 | Resin for removing ligand anions in water, preparation method thereof and zero wastewater regeneration method |
-
1989
- 1989-05-25 CN CN89103379A patent/CN1011403B/en not_active Expired
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8617398B2 (en) | 1996-08-12 | 2013-12-31 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| US8641905B2 (en) | 1996-08-12 | 2014-02-04 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| US8758720B2 (en) | 1996-08-12 | 2014-06-24 | Debasish Mukhopadhyay | High purity water produced by reverse osmosis |
| US9073763B2 (en) | 1996-08-12 | 2015-07-07 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
| US9428412B2 (en) | 1996-08-12 | 2016-08-30 | Debasish Mukhopadhyay | Method for high efficiency reverse osmosis operation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1039569A (en) | 1990-02-14 |
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