CN101759310A - Double-chamber full-chamber bed desalted water treatment method - Google Patents
Double-chamber full-chamber bed desalted water treatment method Download PDFInfo
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- CN101759310A CN101759310A CN201010045625A CN201010045625A CN101759310A CN 101759310 A CN101759310 A CN 101759310A CN 201010045625 A CN201010045625 A CN 201010045625A CN 201010045625 A CN201010045625 A CN 201010045625A CN 101759310 A CN101759310 A CN 101759310A
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Abstract
The invention discloses a double-chamber full-chamber bed desalted water treatment method, which comprises the operating steps that: raw water is filtered by a mechanical filter, the obtained water enters the cation bed of a double-chamber full-chamber bed from the bottom after suspended impurities in the water are removed, sequentially passes through weakly acidic resin and strongly acidic resin, is fed into the anion bed of the double-chamber full-chamber bed from the bottom by a pump after carbon dioxide is removed through a decarburization tower, sequentially passes through weakly alkali resin and strongly alkali resin, simultaneously hydrogen ions produced by the cation bed and hydroxyl ions produced by the anion bed are automatically neutralized, and acceptable desalted water is obtained and stored in a desalted water tank for external use. The method of the invention has the advantages that the utilization ratio of acid and alkali is above 99.99 percent, the waste water satisfies the standard and can be directly emitted, the process is short, the equipment investment and the operating cost are low, the amount of waste water is small, the water quality is good and the operation is simple and convenient.
Description
Technical field
The invention belongs to the Treatment of Industrial Water technical field, specifically is a kind of double-chamber full-chamber bed desalted water treatment method.
Background technology
The desalination process of service water can be divided into three kinds of ion exchange method, reverse osmosis method and electroosmose processs.Electroosmose process prematurity still in engineering is used generally can not be used separately; Though reverse osmosis method does not have spent acid, salkali waste discharging, has drawbacks such as wastewater flow rate is big, operation and maintenance cost height, effluent quality is relatively poor, water-yielding capacity is lower, is only applicable to the high former water treatment of saltiness; Traditional ion exchange method has fixed bed, floating bed, full chamber bed, two chambers floating bed, two chamber kinds of processes such as " floating bed+full chamber beds ", has to some extent all that a large amount of spent acid salkali waste dischargings, acid and alkali consumption height, resin life are short, the backwash water yield is big, troublesome poeration, production cost be than problems such as height.
Summary of the invention
Technical problem to be solved by this invention provides a kind of double-chamber full-chamber bed desalted water treatment method that the spent acid salkali waste discharges, effluent quality is good, acid-base consumption is low, blowdown is few, treatment capacity is big, resin life is long, running cost is low, simple to operate that do not have.
The present invention solves the problems of the technologies described above with following technical scheme: the treatment step of double-chamber full-chamber bed desalted water treatment method of the present invention is: former water filters through mechanical filter, entering structure from the bottom behind the elimination suspended impurity is double-chamber full-chamber bed sun bed, successively by slightly acidic and highly acidic resin decationize, remove behind the carbonic acid gas with pump delivery through decarbonizing tower again, entering structure from the bottom is double-chamber full-chamber bed cloudy bed, remove negatively charged ion by weakly alkaline and basic resin successively, the hydroxide ion that hydrogen ion that sun bed produces and cloudy bed are produced neutralizes voluntarily, makes qualified de-mineralized water and enters the desalination tank and store and be for external application.
Highly acidic resin is filled in the last chamber of described sun bed, weakly acidic resin is filled in following chamber, and basic resin is filled in the last chamber of cloudy bed, and weakly base resin is filled in following chamber, two all is furnished with the porous plate water distributor in sun bed and the cloudy bed tank body, middlely with the porous plate water distributor two kinds of resins is separated.
Sun bed with hydrochloric acid or sulfuric acid as regenerator, its regeneration is the counter flow series regeneration, and promptly regenerator enters the sun bed from the top, and flow through successively highly acidic resin and weakly acidic resin exchange, regeneration waste liquid directly enters neutralization tank from the bottom of sun bed, and the regeneration waste liquid pH value is greater than 3; Cloudy bed with caustic soda as regenerator, its regeneration is counter flow series regeneration, and promptly regenerator enters cloudy bed from the top, and flow through successively basic resin and weakly base resin exchange, regeneration waste liquid directly enters neutralization tank from the bottom of cloudy bed, and the regeneration waste liquid pH value is lower than 11.
The sun bed is as if being regenerator with hydrochloric acid, and its regenerated liquid concentration (mass percent, down together) is 1～4%, and flow velocity is 3～6 meters/hour; The sun bed then adopts two step method of reproduction as if being regenerator with sulfuric acid, and the first step regenerated liquid concentration is 0.5～0.7%, and flow velocity is 5～7 meters/hour, and the acid amount is 70～80%; The second step regenerated liquid concentration is 1.2～1.5%, and flow velocity is 5～7 meters/hour, and the acid amount is 20～30%; Cloudy bed is a regenerator with the caustic soda, and regenerated liquid concentration is 1～4%, and flow velocity is 3～6 meters/hour; Regenerated liquid flow and concentration take into account acid by regeneration de-mineralized water flow or the alkali under meter is regulated.
It is the end of run greater than 200mg/L that the sun bed contains the sodium amount with water outlet, and it is the end of run greater than 100mg/L that cloudy bed contains silica volume with water outlet.
Sun bed of the present invention and cloudy bed are in operational process, and resin is full of whole chamber, maintains static during operation, solved the floating bed resin broken problem of rolling, so resin life are longer; Pending water enters from bottom, following chamber, and suspended substance is trapped within down the bottom, chamber, can be reproduced and replace waste water to rinse out, and therefore can cancel fixed bed backwash operation, saved a large amount of fresh backwash water, so wastewater flow rate still less.
When regeneration sun bed acid solution flow through successively strongly-acid and weakly acidic resin, the remaining spent acid that highly acidic resin exchange back produces can be absorbed by weakly acidic resin fully, the regeneration waste liquid pH value is 3～7, corresponding hydrochloric acid mass percent concentration is 0～0.00365%, the sulfuric acid mass percent concentration is 0～0.0098%, illustrates that the acid-utilising rate can be up to more than 99.99%; Flow through successively strong basicity and weakly base resin of alkali lye during cloudy bed regeneration, the remaining salkali waste that basic resin exchange back produces can be absorbed by weakly base resin fully, the regeneration waste liquid pH value is 7～11, corresponding caustic soda mass percent concentration is 0～0.004%, illustrates that the alkali utilization ratio can be up to more than 99.99%.Therefore basic " zero release " that realizes regenerating spent acid, salkali waste, not only solve fixed bed, floating bed, full chamber bed, two chambers floating bed, a large amount of spent acid of two chamber traditional desalination process such as " floating bed+full chamber beds ", a salkali waste discharging difficult problem, also reduced running cost significantly.
The inventive method is compared and is had the following advantages with conventional ion exchange desalination method, reverse osmosis desalination method:
(1) to former water wide accommodation, saltiness all can adopt less than 700mg/L.
Acid when (2) regenerating, alkali utilization ratio reach more than 99.99%, realize " zero release " of spent acid, salkali waste substantially, so its soda acid unit consumption are low, and running cost is low; And conventional ion exchange desalination method soda acid utilization ratio generally only is 20～70%, and soda acid unit consumption height produces a large amount of spent acid, salkali waste, the running cost height.
(3) conventional ion exchange desalination method must use activated charcoal filter to remove organism and heavy metal ion, prevents the poisoning of positive resin heavy metal poisoning and negative resin organism, but poor effect.And but the present invention utilizes double-chamber full-chamber bed slightly acidic and weakly base resin active adsorption and desorption heavy metal ion and organism, prevent resin poison, so resin life is long, and can cancels activated charcoal filter, when shortening technology, facility investment and gac working cost have also been reduced.
(4) wastewater flow rate is few, conventional fixed bed wastewater rate is generally 10%, reverse osmosis is generally 35%, and the present invention adopts and double-chamber full-chamber bedly has only 3%, because double-chamber full-chamber bed desalination method utilization regeneration and displacement waste water replace fresh water to carry out backwash, cancel the backwash operation, saved a large amount of fresh backwash water.
(5) spent acid of the inventive method regeneration minute quantity that produces can neutralize in the waterways voluntarily, direct qualified discharge after the neutralization tank buffering.The conventional ion switching method then produces a large amount of spent acid solutions, waste lye must be sought in alkali lye, the acid solution in addition and could discharge.
(6) the inventive method is in treating processes, former water is through slightly acidic and two kinds of resins of strongly-acid of sun bed, decationized Y sieve water is through strong basicity and two kinds of resin secondary treatments of weakly alkaline of cloudy bed, therefore effluent quality is better, specific conductivity is 0.1～10 μ s/cm during normal the operation, dioxide-containing silica is 0.5～100 μ g/L, and going out the water hardness is 0.
(7) resin is damaged few, is difficult for poisoning long service life.
(8) cycle of operation is long.
(9) flow process advantages of simple, simple and compact equipment structure, easy handling is safeguarded.
Description of drawings
Fig. 1 is the process flow sheet of treatment process of the present invention.
Embodiment
As shown in Figure 1, the technical process of treatment process of the present invention is: former water is through sand-bed filter, enter positive from the bottom after eliminating suspended impurity, the sun bed is double-chamber full-chamber bed, it comprises chamber and following chamber, highly acidic resin is filled in last chamber, weakly acidic resin is filled in following chamber, two all is furnished with the porous plate water distributor in the tank body, the centre separates two kinds of resins with the porous plate water distributor, former water removes calcium in anhydrating by slightly acidic and highly acidic resin successively, magnesium, sodium, positively charged ion such as potassium and ferrimanganic (discharging hydrogen ion simultaneously) back is from the top water outlet, remove behind the carbonic acid gas with pump delivery through decarbonizing tower again, enter cloudy bed from the bottom, cloudy bed also is double-chamber full-chamber bed, it includes chamber and following chamber, basic resin is filled in last chamber, weakly base resin is filled in following chamber, two is furnished with the porous plate water distributor in the tank body, the centre separates two kinds of resins with the porous plate water distributor, decationized Y sieve water removes sulfate radical in anhydrating by weakly alkaline and basic resin successively, the chlorine root, negatively charged ion such as silicate and nitrate radical (discharging hydroxide ion simultaneously) back is from the top water outlet, the hydroxide ion that hydrogen ion that sun bed produces and cloudy bed are produced neutralizes voluntarily, makes qualified de-mineralized water (in case of necessity again through overmulling bed secondary desalination) and enters the desalination tank and store and be for external application.
Sun bed as regenerator, adopts the counter flow series regeneration with hydrochloric acid or sulfuric acid, and promptly regenerator enters the sun bed from the top, and flow through successively highly acidic resin and weakly acidic resin exchange, and exchange back waste liquid directly enters neutralization tank at the bottom of jar.If with hydrochloric acid is regenerator, its regenerated liquid concentration (mass percent, down together) is 1～4% proportion by subtraction, and flow velocity is 3～6 meters/hour.If with sulfuric acid is regenerator, then adopt two step method of reproduction, the first step regenerated liquid concentration is 0.5～0.7%, and flow velocity is 5～7 meters/hour, and the acid amount is 70～80%; The second step regenerated liquid concentration is 1.2～1.5%, and flow velocity is 5～7 meters/hour, and the acid amount is 20～30%.Strict control acid intake amount during regeneration guarantees that regeneration waste liquid PH is not less than 3.Regenerated liquid flow and concentration are regulated by regeneration de-mineralized water under meter and sour under meter.
Cloudy bed is a regenerator with the caustic soda, also adopts the counter flow series regeneration, and promptly regenerator enters cloudy bed from the top, flow through successively basic resin and weakly base resin exchanges, exchange back waste liquid directly enters neutralization tank at the bottom of jar, its regenerated liquid concentration is 1～4%, and flow velocity is 3～6 meters/hour.Alkali number is advanced in strict control during regeneration, guarantees that regeneration waste liquid PH is not higher than 11.Regenerated liquid flow and concentration are taken into account the alkali under meter by regeneration de-mineralized water flow and are regulated.
Sun bed that treatment process of the present invention adopts and cloudy bed are double-chamber full-chamber bed, and chamber and following chamber are full chamber bed on it, and the resin of use is the various resins that water treatment is used, and resin is full of whole chamber with deploying type.Resin maintained static when system moved, and pending water enters from bottom, following chamber, and suspended substance is trapped within down the bottom, chamber, can be reproduced and replace waste water to rinse out, and therefore can cancel fixed bed backwash operation, has saved a large amount of fresh backwash water.So resin life is longer, and wastewater flow rate still less.
It is the end of run greater than 200mg/L that the sun bed that the present invention adopts contains the sodium amount with water outlet, and it is the end of run greater than 100mg/L that cloudy bed contains silica volume with water outlet.Can adopt on-line monitoring or manual assays to monitor water quality.
Below be the case history of using treatment process of the present invention:
1. South of Guangxi chemical industry limited liability company adopts the comparison example of conventional processes and the processing of application the inventive method as follows:
Two cover Φ 1500mm * H5500mm fixed beds of original system, the sun bed is loaded 001 * 7 highly acidic resin, cloudy bed is loaded 201 * 7 basic resins, separate unit design water production rate is 35 tons/hour, and the actual water production rate of separate unit is about 32 tons/hour, original water hardness is 3～10mmol/L, and the sun bed adopts the regeneration of hydrochloric acid of 3% (mass percent concentration), and renovation process is low flow velocity counter-current regeneration; Cloudy bed adopts the caustic soda regeneration of 3% (mass percent concentration), and renovation process is low flow velocity counter-current regeneration.By the data that in October, 2009, production report provided, a sun bed actual motion cycle is about 15～19 hours, and the acid consumption is 3.45 kilograms of/ton water, and the water outlet sodium ions content is about 100～300 μ g/L.The cloudy bed actual motion cycle is about 32～40 hours, and alkaline consumption is 4.68 kilograms of/ton water, goes out water conductivity and is about 0.8～10 μ s/cm.Because the soda acid utilization ratio only is 10～15%, a large amount of spent acid, salkali waste discharging cause severe environmental pollution, and wastewater rate is also up to more than 10%.
The cover double-chamber full-chamber bed desalted water system (promptly adopting treatment process of the present invention) that starts in November, 2009, specification of equipment is Φ 1500 * H5500mm, 001 * 7 highly acidic resin is loaded in the last chamber of sun bed, following chamber filling D113 weakly acidic resin; 201 * 7 basic resins are loaded in the last chamber of cloudy bed, the D301 weakly base resin is loaded in following chamber, separate unit design water production rate is 40 tons/hour, the sun bed adopts the regeneration of hydrochloric acid of 3% (mass percent concentration), renovation process is counter flow series regeneration, the regenerating spent acid pH value is 4～7, illustrates that content of hydrochloric acid is 0～0.000365% in the waste liquid, and the acid-utilising rate reaches more than 99.999%; Cloudy bed adopts the caustic soda regeneration of 3% (mass percent concentration), and renovation process is counter flow series regeneration, and regeneration salkali waste pH value is 7～10, illustrates that caustic soda content is 0～0.0004% in the waste liquid, and the alkali utilization ratio reaches more than 99.999%.The actual water production rate of sun sheet platform is 40 tons/hour, and the actual motion cycle is about 65 hours, and the water outlet sodium ions content is about 20～150 μ g/L, and the acid consumption is lower than 0.6 kilogram of/ton water.The actual water production rate of cloudy sheet platform is 40 tons/hour, and the actual motion cycle is about 105 hours, and alkaline consumption is lower than 0.15 kilogram of/ton water, goes out water conductivity and is about 0.1～1 μ s/cm.Do not have spent acid, salkali waste discharging after putting into operation, wastewater rate drops to below 3%.
2. Lanxing Chemical New Material Co., Ltd. Guangxi branch office uses the embodiment of treatment process of the present invention:
The cover double-chamber full-chamber bed desalted water system that starts in July, 2009 of the said firm, specification of equipment is Φ 1500 * H4270mm, and 001 * 7 highly acidic resin is filled in the last chamber of sun bed, and the D113 weakly acidic resin is filled in following chamber; 201 * 7 basic resins are filled in the last chamber of cloudy bed, and the D301 weakly base resin is filled in following chamber, and separate unit design water production rate is 50 tons/hour, and original water hardness is 3～5mmol/L.It is regenerator that the sun bed adopts sulfuric acid, adopts two step method of reproduction, and the first step regeneration concentration is 0.5～0.7% (mass percent concentration), and flow velocity is 5～7 meters/hour, and the acid amount is 70～80%; Second step regeneration concentration is 1.2～1.5% (mass percent concentrations), flow velocity is 5～7 meters/hour, the acid amount is 20～30%, renovation process is counter flow series regeneration, the regeneration waste liquid pH value is 3～7, corresponding sulfuric acid mass percent concentration is 0～0.0098%, illustrates that the acid-utilising rate can be up to more than 99.99%.It is regenerator that cloudy bed adopts the caustic soda of 3% (mass percent concentration), flow velocity is 3～6 meters/hour, and renovation process is counter flow series regeneration, and the regeneration waste liquid pH value is 7～11, corresponding caustic soda mass percent concentration is 0～0.004%, illustrates that the alkali utilization ratio can be up to more than 99.99%.The actual water production rate of sun sheet platform is 50 tons/hour, and the actual motion cycle is about 24 hours, and going out the water hardness is 0mmol/L, and the acid consumption is about 0.4 kilogram of/ton water.The actual water production rate of cloudy sheet platform is 50 tons/hour, and the actual motion cycle is about 48 hours, and alkaline consumption is about 0.12 kilogram of/ton water, goes out water conductivity and is about 0.2～10 μ s/cm.Do not have spent acid, salkali waste discharging after putting into operation, wastewater rate drops to below 3%.
Claims (5)
1. double-chamber full-chamber bed desalted water treatment method, the treatment step that it is characterized in that this method is: former water filters through mechanical filter, entering structure from the bottom behind the elimination suspended impurity is double-chamber full-chamber bed sun bed, successively by slightly acidic and highly acidic resin decationize, remove behind the carbonic acid gas with pump delivery through decarbonizing tower again, entering structure from the bottom is double-chamber full-chamber bed cloudy bed, remove negatively charged ion by weakly alkaline and basic resin successively, the hydroxide ion that hydrogen ion that sun bed produces and cloudy bed are produced neutralizes voluntarily, makes qualified de-mineralized water and enters the desalination tank and store and be for external application.
2. double-chamber full-chamber bed desalted water treatment method according to claim 1, it is characterized in that: highly acidic resin is filled in the last chamber of described sun bed, weakly acidic resin is filled in following chamber, basic resin is filled in the last chamber of cloudy bed, weakly base resin is filled in following chamber, a positive bed and a cloudy bed tank body two all are furnished with the porous plate water distributor, and the centre separates two kinds of resins with the porous plate water distributor.
3. double-chamber full-chamber bed desalted water treatment method according to claim 1 and 2, it is characterized in that: sun bed with hydrochloric acid or sulfuric acid as regenerator, its regeneration is counter flow series regeneration, be that regenerator enters the sun bed from the top, flow through successively highly acidic resin and weakly acidic resin exchanges, regeneration waste liquid directly enters neutralization tank from the bottom of sun bed, and the regeneration waste liquid pH value is greater than 3; Cloudy bed with caustic soda as regenerator, its regeneration is counter flow series regeneration, and promptly regenerator enters cloudy bed from the top, and flow through successively basic resin and weakly base resin exchange, regeneration waste liquid directly enters neutralization tank from the bottom of cloudy bed, and the regeneration waste liquid pH value is lower than 11.
4. double-chamber full-chamber bed desalted water treatment method according to claim 1 is characterized in that: the sun bed is as if being regenerator with hydrochloric acid, and its regenerated liquid concentration is 1～4%, and flow velocity is 3～6 meters/hour; The sun bed then adopts two step method of reproduction as if being regenerator with sulfuric acid, and the first step regenerated liquid concentration is 0.5～0.7%, and flow velocity is 5～7 meters/hour, and the acid amount is 70～80%; The second step regenerated liquid concentration is 1.2～1.5%, and flow velocity is 5～7 meters/hour, and the acid amount is 20～30%; Cloudy bed is a regenerator with the caustic soda, and regenerated liquid concentration is 1～4%, and flow velocity is 3～6 meters/hour; Regenerated liquid flow and concentration take into account acid by regeneration de-mineralized water flow or the alkali under meter is regulated.
5. according to claim 1 or 2 or 3 or 4 described double-chamber full-chamber bed desalted water treatment methods, it is characterized in that: it is the end of run greater than 200mg/L that the sun bed contains the sodium amount with water outlet, and it is the end of run greater than 100mg/L that cloudy bed contains silica volume with water outlet.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102653426A (en) * | 2011-03-03 | 2012-09-05 | 彭悦 | Demineralized water device of six-tower fluidized bed |
| CN103739114A (en) * | 2013-12-27 | 2014-04-23 | 陕西大唐新能电力设计有限公司 | Boiler water treatment system |
| CN104291484A (en) * | 2014-09-30 | 2015-01-21 | 杭州安耐杰科技有限公司 | High-efficiency environment-friendly desalted water production method |
| CN104986825A (en) * | 2015-07-07 | 2015-10-21 | 杭州安耐杰科技有限公司 | Wastewater treatment process for ion exchange system |
| CN110548548A (en) * | 2019-10-12 | 2019-12-10 | 唐可 | Double-chamber ion exchanger in-situ regeneration process, device and water treatment system |
| CN111392913A (en) * | 2020-04-24 | 2020-07-10 | 莱特莱德（北京）环境技术股份有限公司 | System and method for advanced treatment of PVC centrifugal mother liquor waste liquid |
-
2010
- 2010-01-12 CN CN201010045625A patent/CN101759310A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102653426A (en) * | 2011-03-03 | 2012-09-05 | 彭悦 | Demineralized water device of six-tower fluidized bed |
| CN103739114A (en) * | 2013-12-27 | 2014-04-23 | 陕西大唐新能电力设计有限公司 | Boiler water treatment system |
| CN104291484A (en) * | 2014-09-30 | 2015-01-21 | 杭州安耐杰科技有限公司 | High-efficiency environment-friendly desalted water production method |
| CN104986825A (en) * | 2015-07-07 | 2015-10-21 | 杭州安耐杰科技有限公司 | Wastewater treatment process for ion exchange system |
| CN110548548A (en) * | 2019-10-12 | 2019-12-10 | 唐可 | Double-chamber ion exchanger in-situ regeneration process, device and water treatment system |
| CN110548548B (en) * | 2019-10-12 | 2024-03-29 | 唐可 | In-situ regeneration process and device for double-chamber ion exchanger and water treatment system |
| CN111392913A (en) * | 2020-04-24 | 2020-07-10 | 莱特莱德（北京）环境技术股份有限公司 | System and method for advanced treatment of PVC centrifugal mother liquor waste liquid |
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Open date: 20100630 |