CN104609642A - Denitration method for regeneration brine by cycle utilization of ion exchange resin - Google Patents
Denitration method for regeneration brine by cycle utilization of ion exchange resin Download PDFInfo
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Abstract
The invention belongs to the environment protection and water treatment fields, and provides a denitration method for regeneration brine by cycle utilization of ion exchange resin. By employing regeneration brine, two phases of regeneration on failure anion exchange resin after processing nitrate pollution raw water are carried out, regeneration brine is collected by segmentation, sulfate and nitrate are removed, so that resin regeneration can be realized. According to the invention, nitrate and sulfate in the regeneration brine can be removed, unfavorable influence of organic by-product generated by biochemical treatment can be reduced, active carbon consumption is reduced, and cost of regeneration brine by cycle utilization of resin can be reduced.
Description
Technical field
The invention belongs to environment protection and water treatment field, a kind of method of recycle ion exchange resin denitration regenerate brine is provided.
Background technology
Underground water is important drinking water source in Northern Part of China, but its azotate pollution is heavier.Nitrate enters in human body, can change the physiology microenvironment of intestinal tract, be unfavorable for the activity of beneficial functions flora; Also be combined with oxyphorase after may being converted into nitrite, make it lose oxygen carrying capacity; Or be combined with organic amine material, generate the objectionable impurities having carcinogenesis.Therefore, drink nitric acid superstandard drinking water, the health of harmful to human.In addition, the azotate pollution of water can reduce quality of vegetable, is also unfavorable for the healthy growth of animal in aquatic products and livestock and poultry cultivation.Therefore, compare the northern area of shortage at surface water, groundwater azotate pollution all brings adverse influence to the life of the mankind and production, urgently administers.
In water, the minimizing technology of nitrate mainly contains physico-chemical processes, chemical method and biochemical process.Physico-chemical processes mainly contains distillation, electrodialysis, reverse osmosis, ion-exchange etc.Wherein, former three does not have selectivity, except also been removed other element useful to human body in water while nitre; Ion exchange method is quick, is easy to Automated condtrol, but produces high nitre high-salt wastewater.In fact, all physics chemistry method is transfer and enrichment nitrate just, and the nitrate wastewater of generation needs to carry out suitable subsequent disposal, environment of being allowed for access.
Chemical reduction can be reductive agent with the active metal such as aluminium, iron simple substance except nitre method, can be also reductive agent with hydrogen, formic acid etc., reduce nitrate under catalyst action.No matter be active metal reduction method, or catalytic reduction method, all easily form nitrite or ammonium class by product, in practical application, also have many restrictions.
Biological denitrification is denitrifying bacterium is the process of nitrogen by nitrate reduction, comprises autotrophy and heterotrophic denitrification two type.Wherein, autotrophic denitrification is using the inorganics such as hydrogen, elemental sulfur as electron donor, and denitrification rate is comparatively slow, but it is better to go out water quality.But, hydrogen autotrophic denitrification due to hydrogen solubility low, explosive, large-scale application is difficult; Sulphur autotrophic denitrification can produce sulfate radical and acidity, is only suitable for treatment of nitric acid salt and exceeds standard not serious and that sulfate concentration is not high former water.Heterotrophic denitrification is using organic carbon source as electron donor, and denitrification rate is very fast, but carbon source interpolation requires high, and excessive meeting is residual and increase subsequent disposal difficulty, adds deficiency and easily causes water outlet nitrite to be accumulated.
The respective advantage playing ion exchange method and biochemical process can be combined, with the nitrate in the former water of ion exchange method transfer enrichment, then thoroughly remove the high concentration nitrate in ion exchange resin regeneration salt solution in biochemical mode.But, in the hinterland that rainwash is less, regenerate brine, except after nitre or can not outer row easily, because outer salt discharge water is not easy to be taken away by rainwash, but finally enters underground mostly, thus the salinization of promotion soil and groundwater.
Therefore, in hinterland, recycle ion exchange resin denitration regenerate brine, could reduce its disadvantageous effect to environment to greatest extent.Accomplish this point, need the accumulation controlling vitriol in regenerate brine; Need to remove the organic by-products produced in biological denitrification process; Need to remove other objectionable impurities of possibility enrichment in regenerate brine, such as arsenate.Only in this way, recycle regenerate brine just can not pollute resin and reduce resin except nitre ability.
Sulfate radical minimizing technology in regenerate brine has three kinds substantially: biological sulphate reduction, calcium sulfate precipitation and barium sulfate precipitate.Sulfate reduction method is only suitable for the situation that in regenerate brine, sulfate concentration is not high; It is a contradiction that calcium sulfate precipitation is removed between vitriol and calcium ion remnants, and requires that pH neutrality is even acid; The effect that barium sulfate precipitate removes sulfate radical is better than calcium sulfate precipitation, but cost is higher.
During heterotrophic denitrification process denitration regenerate brine, nitrate concentration is generally at more than 30mmol/L, and corresponding organic carbon source demand is also at more than 1500mg BOD/L.In this case, the organic by-products concentration that in water outlet, bacterial metabolism is formed is also higher, and process by conventional active carbon adsorption, effect is unsatisfactory, and carbon, C regeneration cost is higher.
Summary of the invention
In order to reduce ion exchange resin except nitre regenerate brine is to the disadvantageous effect of environment, the invention provides a kind of method of recycle ion exchange resin denitration regenerate brine.
For achieving the above object, the technical solution adopted in the present invention is:
A kind of method of recycle ion exchange resin denitration regenerate brine: adopt regenerate brine, the anionite-exchange resin lost efficacy after treatment of nitric acid salt polluted raw is carried out to the regeneration in two stages, Fractional Collections regenerated salt solution, and the sulfate and nitrate removed wherein, again for resin regeneration.
Wherein, in regenerate brine, the concentration of villaumite is 0.1-1.0mol/L, and the concentration of supercarbonate is 0.05-0.5mol/L, and the total salt concentration of villaumite and supercarbonate is 0.3-1.5mol/L.
Described, first carry out first stage resin regeneration process, and terminate when the concentration of regenerated sulfate anion in brine system is between 60-120mmol/L, collecting gained is first stage regenerated salt solution; Then proceed subordinate phase plastic resin treatment, stop as the concentration 2-10mmol/L of nitrate radical in regenerated salt solution, collecting gained is subordinate phase regenerated salt solution.
Described, the acetic acid as denitrifying carbon source is added in described first stage regenerated salt solution, make pH<7.0, then calcium chloride is added, make the remaining 10-20mmol/L of calcium ion, remove part sulfate radical with calcium sulfate precipitation form, then first stage regenerated salt solution mixes with subordinate phase regenerated salt solution, utilize the bicarbonate radical basicity in subordinate phase waste water to form precipitation of calcium carbonate, make regenerated salt solution calcium ion residual concentration <3mmol/L.
The regenerated salt solution of described calcium ion residual concentration <3mmol/L is used for biological denitrification process, in denitrification process, 80-90%(and 10-20% that organic carbon source adds total amount carbon source needed for all nitrate of regenerated salt solution of removal calcium ion residual concentration <3mmol/L is not enough), to reduce the formation of organic by-products in biological treatment process, and add the sulfide of 1-5mmo/L, make denitrification process terminate rear nitrite residual concentration <1.0mmol/L.
Wherein, add calcium chloride in regenerated salt solution after biological denitrification process, its molar equivalent added is the 40-60% of denitrification process nitrate removal molar equivalent, the Speleothem precipitation adsorption organism wherein of formation, then after filtering, sterilizing, again for resin regeneration.
Special purpose device:
Device comprises former pond (1), ion exchange resin column (2), ion-exchange outlet sump (3), resin regeneration pump sump (4), resin regeneration first stage outlet sump (5), calcium sulfate precipitation pond (6), resin regeneration subordinate phase outlet sump (7), precipitation of calcium carbonate pond (8), biological denitrification reaction system (9), precipitation of calcium carbonate adsorption tank (10), strainer (11), sterilizer (12), regenerate brine storage pool (13), resin cleaning pump sump (14) and resin cleaning outlet sump (15),
Wherein, former pond (1) water outlet, resin regeneration first stage outlet sump (5) water-in, resin regeneration subordinate phase outlet sump (7) water-in are communicated with one end of ion exchange resin column (2) is parallel respectively by the valvular pipeline of band with resin cleaning outlet sump (15) water-in; Ion-exchange outlet sump (3) water-in, resin regeneration pump sump (4) water outlet are communicated with the other end of ion exchange resin column (2) is parallel respectively by the valvular pipeline of band with resin cleaning pump sump (14) water outlet;
Calcium sulfate precipitation pond (6), precipitation of calcium carbonate pond (8), biological denitrification reaction system (9), precipitation of calcium carbonate adsorption tank (10), strainer (11), sterilizer (12), regenerate brine storage pool (13) are connected by pipeline successively with resin regeneration pump sump (4); Described calcium sulfate precipitation pond (6) is connected with resin regeneration first stage outlet sump (5) water outlet by pipeline, and precipitation of calcium carbonate pond (8) are connected by pipeline with resin regeneration subordinate phase outlet sump (7) water outlet.
Described biological denitrification reaction system (9) comprises pressure balanced device in denitrification reactor, denitrification reactor, fluid-tight pond; In reactor, the inlet mouth of pressure balanced device is communicated with denitrification reactor upper end by pipeline, and its air outlet communicates with bottom denitrification reactor with by pipeline, and its excessive gas port is connected with sebific duct, in the other end immersion fluid-tight pond of sebific duct under liquid level.
The present invention is advantageously:
1. the present invention is while the nitrate removed in resin regeneration effluent brine and vitriol, also greatly reduces the disadvantageous effect of the organic by-products that biological denitrification produces, reduces the cost of recycle resin regeneration brine.
2. the present invention utilizes the acetic acid as carbon source to carry out acidifying first stage regenerated salt solution, removes sulfate radical create conditions for precipitation; The precipitation of calcium carbonate formed after the mixing of first and second stage regeneration effluent brine, reduces calcium ion remaining, is beneficial to the operation of biological denitrification.
3. the denitrification that carbon source is limited is conducive to improving utilization of carbon source rate, reduces the formation of organic by-products.
4. the calcium chloride that the basicity utilizing denitrification process to produce and external source are added, generate Speleothem, flocculation sediment removes the water-soluble organic by-products that denitrification process produces, and reduces activated carbon consumption.
Accompanying drawing explanation
Fig. 1 is the device of the ion exchange resin denitration regenerate brine circulation utilization method that the embodiment of the present invention provides.
Embodiment
Embodiment 1
The device of recycle ion exchange resin denitration regenerate brine comprises: former pond (1), ion exchange resin column (2), ion-exchange outlet sump (3), resin regeneration pump sump (4), resin regeneration first stage outlet sump (5), calcium sulfate precipitation pond (6), resin regeneration subordinate phase outlet sump (7), precipitation of calcium carbonate pond (8), biological denitrification reaction system (9), precipitation of calcium carbonate adsorption tank (10), strainer (11), sterilizer (12), regenerate brine storage pool (13), resin cleaning pump sump (14) and resin cleaning outlet sump (15).Wherein, former pond (1) water outlet, resin regeneration first stage outlet sump (5) water-in, resin regeneration subordinate phase outlet sump (7) water-in are communicated with one end of ion exchange resin column (2) is parallel respectively by the valvular pipeline of band with resin cleaning outlet sump (15) water-in; Ion-exchange outlet sump (3) water-in, resin regeneration pump sump (4) water outlet are communicated with the other end of ion exchange resin column (2) is parallel respectively by the valvular pipeline of band with resin cleaning pump sump (14) water outlet.Calcium sulfate precipitation pond (6), precipitation of calcium carbonate pond (8), biological denitrification reaction system (9), precipitation of calcium carbonate adsorption tank (10), strainer (11), sterilizer (12), regenerate brine storage pool (13) are connected by pipeline successively with resin regeneration pump sump (4); Described calcium sulfate precipitation pond (6) is connected with resin regeneration first stage outlet sump (5) water outlet by pipeline, and precipitation of calcium carbonate pond (8) are connected by pipeline with resin regeneration subordinate phase outlet sump (7) water outlet.
The former water of ion exchange resin treatment: ion exchange column (2) high 100cm, inside fills out the 717 type anionite-exchange resin regenerated.Former water pH value is 7.3, and nitrate concentration is 3.2mmol/L, and sulfate concentration is 2.1mmol/L, and chlorine ion concentration is 0.8mmol/L.Open the valve being communicated with former pond (1) water outlet and ion-exchange outlet sump (3) water-in, under 20-24 DEG C of condition, with the former water of flow velocity process of 13.5BV/h.Move to 14 hours, the nitrate concentration in water outlet, more than 0.7mmol/L, is closed above-mentioned two valves, is entered the resin regeneration stage.
Ion exchange resin regeneration and cleaning: resin regeneration regenerate brine used contains the potassium sulfate of the sodium-chlor of 0.5N, the sodium bicarbonate of 0.07N and 0.1N.First opening the valve being communicated with resin regeneration pump sump (4) water outlet and resin regeneration first stage outlet sump (5) water-in, is that 4.5BV/h carries out first stage resin regeneration with flow velocity.After 1 hour, when regenerated sulfate anion in brine system concentration is 110mmol/L, close the valve being communicated with resin regeneration first stage outlet sump (5) water-in, open the valve being communicated with resin regeneration subordinate phase outlet sump (7) water-in, carry out subordinate phase resin regeneration with the flow velocity of 4.5BV/h.After 2 hours, the nitrate concentration in regenerated salt solution is 6.5mmol/L, closes the valve being communicated with resin regeneration pump sump (4) water outlet and resin regeneration subordinate phase outlet sump (7) water-in.Open the valve being communicated with resin cleaning pump sump (14) water outlet and resin cleaning outlet sump (15) water-in, former water after spent ion exchange resin process, with the flow velocity of 6BV/h, cleaning resin 1 hour, then close the valve being communicated with resin cleaning pump sump (14) water outlet and resin cleaning outlet sump (15) water-in, complete regeneration of ion-exchange resin and cleaning.
Pre-treatment before the biochemical treatment of regenerated salt solution: the regenerated salt solution that resin regeneration first stage outlet sump (5) collects enters calcium sulfate precipitation pond (6), sulfate concentration is 216mmol/L, first add the acetic acid of 75mmol/L, make pH<7.0, then the calcium chloride of 130mmol/L is added, produce calcium sulfate precipitation, vitriol residual concentration is down between 80-100mmol/L.Then the regenerated salt solution supernatant liquor of calcium sulfate precipitation pond (6) and resin regeneration subordinate phase outlet sump (7) collected mixes in precipitation of calcium carbonate pond (8), utilize the basicity in subordinate phase regenerated salt solution, form precipitation of calcium carbonate, make calcium ion residual concentration in mixed regeneration effluent brine be reduced to below 3mmol/L, complete the pre-treatment before the biochemical treatment of regenerated salt solution.Its supernatant liquor enters biological denitrification reaction system (9).
Biological denitrification removes the nitrate in regenerated salt solution: the denitrification reactor height 100cm of biological denitrification reaction system (9), internal diameter 9cm, and effective volume is 5.4L, with the exchange rate of 45%, and sequencing batch operation under 20-24 DEG C of condition.The inlet mouth of the airbag of a 10L communicates with denitrification reactor upper end, and air outlet communicates with the bottom of denitrification reactor, and the gas port that overflows communicates with the water-immersed silicone tube in one end.Every 10 minutes intervals, carry out the inner circulating aerating of 15 seconds, the pH change in simultaneous buffering denitrification reactor to denitrification reactor with the mixed gas of the carbonic acid gas in airbag and nitrogen.Airbag, also as pressure regulator in reactor, avoids oxygen to enter denitrification reactor when water inlet or draining.Before formal process regenerated salt solution, the denitrifying activated sludge in nitrator (10) first accepts domestication and cultivates.The potassium sulfate that salt solution used contains the sodium-chlor of 0.5mol/L, the sodium bicarbonate of 0.20mol/L and 0.1mol/L is cultivated in domestication, and nitrate concentration is progressively increased to 40,50 and 60mmol/L from 30mmol/L, tames cultivation about 2 weeks under each concentration.Acetic acid add total amount needed for all nitrate of regenerated salt solution of above-mentioned removal calcium ion residual concentration <3mmol/L carbon source 70%, and add 2mmol/L sodium sulphite regulation and control nitrite accumulation.At the end of denitrification, nitrate residual concentration is stabilized in more than 5mmol/L, and nitrite residual concentration is stabilized in below 0.5mmol/L, terminates domestication and cultivates.Then by the biological denitrification system of the having tamed supernatant liquor (namely through pretreated regenerated salt solution) for the treatment of precipitation of calcium carbonate pond (8).Nitrate concentration in supernatant liquor is 38.1mmol/L, remove sulfate radical by second acid for adjusting pH precipitation in calcium sulfate precipitation pond (6) while, also for biological denitrification removes the carbon source that all nitrate with the addition of 80%.Add the sodium sulphite of 2mmol/L in operational process in addition, and utilize carbonic acid gas aeration that pH is maintained between 8.0-9.0.Run after 12 hours, nitrate remnants are stabilized in about 4.8mmol/L, and nitrite remnants are 0.2mmol/L, complete denitrification process.
The aftertreatment of denitrification process: biological denitrification reaction system (9) water outlet enters precipitation of calcium carbonate adsorption tank (10), in well-beaten situation, adds the calcium chloride of 20mmol/L, utilizes the organism in the water outlet of Speleothem precipitation adsorption denitrification.After 1 hour, supernatant liquor, after calcium carbonate activated carbon assembled filter (11) and ozonateur (12) process, enters regenerate brine storage pool (13), and adds the sodium-chlor lost in regenerative process, enter resin regeneration pump sump (4), again for resin regeneration.
Embodiment 2
The structure of resin column is with biological denitrification system architecture and tame identical with embodiment 1.
The former water of ion exchange resin treatment: former water pH value is 7.3, nitrate concentration is 4.2mmol/L, and sulfate concentration is 1.6mmol/L, and chlorine ion concentration is 0.8mmol/L.Open the valve being communicated with former pond (1) water outlet and ion-exchange outlet sump (3) water-in, under 20-24 DEG C of condition, with the former water of flow velocity process of 13.5BV/h.Move to 15 hours, the nitrate concentration in water outlet, more than 0.7mmol/L, is closed above-mentioned two valves, is entered the resin regeneration stage.
Ion exchange resin regeneration and cleaning: resin regeneration regenerate brine used contains the potassium sulfate of the sodium-chlor of 0.5N, the sodium bicarbonate of 0.14N and 0.1N.First opening the valve being communicated with resin regeneration pump sump (4) water outlet and resin regeneration first stage outlet sump (5) water-in, is that 4.5BV/h carries out first stage resin regeneration with flow velocity.After 1 hour, when regenerated sulfate anion in brine system concentration is 108mmol/L, close the valve being communicated with resin regeneration first stage outlet sump (5) water-in, open the valve being communicated with resin regeneration subordinate phase outlet sump (7) water-in, carry out subordinate phase resin regeneration with the flow velocity of 4.5BV/h.After 2.5 hours, the nitrate concentration in regenerated salt solution is 5.4mmol/L, closes the valve being communicated with resin regeneration pump sump (4) and resin regeneration subordinate phase outlet sump (7) water-in.Open the valve being communicated with resin cleaning pump sump (14) water outlet and resin cleaning outlet sump (15) water-in, former water after spent ion exchange resin process, with the flow velocity of 6BV/h, cleaning resin 1 hour, then close the valve being communicated with resin cleaning pump sump (14) water outlet and resin cleaning outlet sump (15) water-in, complete regeneration of ion-exchange resin and cleaning.
Pre-treatment before the biochemical treatment of regenerated salt solution: the regenerated salt solution that resin regeneration first stage outlet sump (5) collects enters calcium sulfate precipitation pond (6), sulfate concentration is 207mmol/L, first add the acetic acid of 150mmol/L, make pH<7.0, then the calcium chloride of 130mmol/L is added, produce calcium sulfate precipitation, vitriol residual concentration is down between 80-100mmol/L.Then the regenerated salt solution supernatant liquor of calcium sulfate precipitation pond (6) and resin regeneration subordinate phase outlet sump (7) collected mixes in precipitation of calcium carbonate pond (8), utilize the basicity in subordinate phase regenerated salt solution, form precipitation of calcium carbonate, make calcium ion residual concentration in mixed regeneration effluent brine be reduced to below 3mmol/L, complete the pre-treatment before the biochemical treatment of regenerated salt solution.Its supernatant liquor enters biological denitrification reaction system (9).
Biological denitrification removes the nitrate in regenerated salt solution: the biological denitrification system of having tamed is for the treatment of the supernatant liquor (namely through pretreated regenerated salt solution) of precipitation of calcium carbonate pond (8).Nitrate concentration in supernatant liquor is 48.3mmol/L, remove sulfate radical by second acid for adjusting pH precipitation in calcium sulfate precipitation pond (6) while, also for biological denitrification removes the carbon source that all nitrate with the addition of 85%.Add the sodium sulfide of 2mmol/L in operational process in addition, and utilize carbonic acid gas aeration that pH is maintained between 8.0-9.0.Run after 16 hours, nitrate remnants are stabilized in about 4.0mmol/L, and nitrite remnants are 0.1mmol/L, complete denitrification process.
The aftertreatment of denitrification process: biological denitrification reaction system (9) water outlet enters precipitation of calcium carbonate adsorption tank (10), in well-beaten situation, adds the calcium chloride of 25mmol/L, utilizes the organism in the water outlet of Speleothem precipitation adsorption denitrification.After 1 hour, supernatant liquor, after calcium carbonate activated carbon assembled filter (11) and ozonateur (12) process, enters regenerate brine storage pool (13), and adds the sodium-chlor lost in regenerative process, enter resin regeneration pump sump (4), again for resin regeneration.
Claims (8)
1. a method for recycle ion exchange resin denitration regenerate brine, is characterized in that:
Adopt regenerate brine, the anionite-exchange resin lost efficacy is carried out to the regeneration in two stages, Fractional Collections regenerated salt solution after treatment of nitric acid salt polluted raw, and remove sulfate and nitrate wherein, again for resin regeneration.
2., by the method for recycle ion exchange resin denitration regenerate brine according to claim 1, it is characterized in that:
In regenerate brine, the concentration of villaumite is 0.1-1.0mol/L, and the concentration of supercarbonate is 0.05-0.5mol/L, and the total salt concentration of villaumite and supercarbonate is 0.3-1.5mol/L.
3., by the method for the recycle ion exchange resin denitration regenerate brine described in claim 1 or 2, it is characterized in that:
First carry out first stage resin regeneration process, and terminate when the concentration of regenerated sulfate anion in brine system is between 60-120mmol/L, collecting gained is first stage regenerated salt solution; Then proceed subordinate phase plastic resin treatment, stop as the concentration 2-10mmol/L of nitrate radical in regenerated salt solution, collecting gained is subordinate phase regenerated salt solution.
4., by the method for recycle ion exchange resin denitration regenerate brine according to claim 3, it is characterized in that:
The acetic acid as denitrifying carbon source is added in described first stage regenerated salt solution, make pH<7.0, then calcium chloride is added, make the remaining 10-20mmol/L of calcium ion, part sulfate radical is removed with calcium sulfate precipitation form, then first stage regenerated salt solution mixes with subordinate phase regenerated salt solution, utilizes the bicarbonate radical basicity in subordinate phase waste water to form precipitation of calcium carbonate, makes regenerated salt solution calcium ion residual concentration <3mmol/L.
5., by the method for recycle ion exchange resin denitration regenerate brine according to claim 4, it is characterized in that:
The regenerated salt solution of described calcium ion residual concentration <3mmol/L is used for biological denitrification process, in denitrification process, 80-90%(and 10-20% that organic carbon source adds total amount carbon source needed for all nitrate of regenerated salt solution of removal calcium ion residual concentration <3mmol/L is not enough), to reduce the formation of organic by-products in biological treatment process, and add the sulfide of 1-5mmo/L, make denitrification process terminate rear nitrite residual concentration <1.0mmol/L.
6., by the method for recycle ion exchange resin denitration regenerate brine according to claim 5, it is characterized in that:
Calcium chloride is added in regenerated salt solution after biological denitrification process, its molar equivalent added is the 40-60% of denitrification process nitrate removal molar equivalent, the Speleothem precipitation adsorption organism wherein formed, then after filtering, sterilizing, again for resin regeneration.
7. a special purpose device for the method for recycle ion exchange resin denitration regenerate brine according to claim 1, is characterized in that:
Device comprises former pond (1), ion exchange resin column (2), ion-exchange outlet sump (3), resin regeneration pump sump (4), resin regeneration first stage outlet sump (5), calcium sulfate precipitation pond (6), resin regeneration subordinate phase outlet sump (7), precipitation of calcium carbonate pond (8), biological denitrification reaction system (9), precipitation of calcium carbonate adsorption tank (10), strainer (11), sterilizer (12), regenerate brine storage pool (13), resin cleaning pump sump (14) and resin cleaning outlet sump (15),
Wherein, former pond (1) water outlet, resin regeneration first stage outlet sump (5) water-in, resin regeneration subordinate phase outlet sump (7) water-in are communicated with one end of ion exchange resin column (2) is parallel respectively by the valvular pipeline of band with resin cleaning outlet sump (15) water-in; Ion-exchange outlet sump (3) water-in, resin regeneration pump sump (4) water outlet are communicated with the other end of ion exchange resin column (2) is parallel respectively by the valvular pipeline of band with resin cleaning pump sump (14) water outlet;
Calcium sulfate precipitation pond (6), precipitation of calcium carbonate pond (8), biological denitrification reaction system (9), precipitation of calcium carbonate adsorption tank (10), strainer (11), sterilizer (12), regenerate brine storage pool (13) are connected by pipeline successively with resin regeneration pump sump (4); Described calcium sulfate precipitation pond (6) is connected with resin regeneration first stage outlet sump (5) water outlet by pipeline, and precipitation of calcium carbonate pond (8) are connected by pipeline with resin regeneration subordinate phase outlet sump (7) water outlet.
8. the special purpose device of the method for recycle ion exchange resin denitration regenerant salt according to claim 7, is characterized in that: described biological denitrification reaction system (9) comprises pressure balanced device in denitrification reactor, denitrification reactor, fluid-tight pond; In reactor, the inlet mouth of pressure balanced device is communicated with denitrification reactor upper end by pipeline, and its air outlet communicates with bottom denitrification reactor with by pipeline, and its excessive gas port is connected with sebific duct, in the other end immersion fluid-tight pond of sebific duct under liquid level.
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| CN109850992A (en) * | 2019-03-29 | 2019-06-07 | 中国科学院沈阳应用生态研究所 | The liquid manure salt ion input integration regulation method and device of facility for prevention and control agricultural soil Secondary Saline |
| CN109850992B (en) * | 2019-03-29 | 2023-09-26 | 中国科学院沈阳应用生态研究所 | Water-fertilizer-salt ion input integrated regulation and control method and device for preventing and controlling secondary salinization of facility agriculture soil |
| EP4103516A4 (en) * | 2020-02-12 | 2023-08-23 | Clean Teq Water Technology Pty Ltd. | A process and a plant |
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