CN2277985Y - Ion exchanging pure water treating device - Google Patents
Ion exchanging pure water treating device Download PDFInfo
- Publication number
- CN2277985Y CN2277985Y CN 96224290 CN96224290U CN2277985Y CN 2277985 Y CN2277985 Y CN 2277985Y CN 96224290 CN96224290 CN 96224290 CN 96224290 U CN96224290 U CN 96224290U CN 2277985 Y CN2277985 Y CN 2277985Y
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- valve
- exchange
- water
- exchange column
- anion
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- Expired - Fee Related
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- Treatment Of Water By Ion Exchange (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model provides an ion exchange pure water treating device. The utility model comprises a base, a cation exchange column, an anion exchange column, a microporous filter and an ultrafiltration filter provided with a bacteria discharge valve, wherein, the cation exchange column and the anion exchange column are arranged on the base, and the microporous filter is provided with a raw water inlet valve and a sewer valve; a water inlet valve, an acid inlet valve. An alkali inlet valve, an outlet and a plurality of crossover valves are arranged on the base, and pipelines respectively communicate the valves with the cation exchange column, the anion exchange column, the microporous filter and the ultrafiltration filter. The utility model has the advantages of low production cost, safe use and long service life; besides, pure water and high pure water of high quality can be produced.
Description
The utility model relates to a kind of pure water treater, particularly be a kind of ion exchange pure water treater.
Existing water is purified, adopt electroosmose process mostly, reverse osmosis method, ion exchange method.
1), electric osmose folding method: be under the DC electric field effect, utilize the selective permeability of ion-exchange membrane can divide dried up in electrolytical principle and produce pure water.The required equipment complex structure, consumed power, water purifying effect is poor, and the expensive gold of institute is many.
2), reverse osmosis method: being impurity and the water sepn of utilizing in the pressure official post water, is a membrane separation technique.Technical sophistication, power consumption are big, the equipment easy break-down, and water purifying effect is poor, and the expensive gold of institute is many.
3), used equipment ion exchange method: ion exchange method be the exchange group that utilizes ion exchange resin because of in have and can remove impurity in the water with the ability of impurity atom exchange in the water.The ion exchange method water purifying effect is good, the desalting efficiency height.But equipment all adopts steel body material and rigid plastics splendid attire ion exchange resin, in producing the pure water process, can't carry out effective monitoring to streamflow regime and ion exchange resin dynamic process, unavoidable channel and the no water subfill situation of producing, influence the water treatment effect, be difficult to the stable aquatic product of ensuring the quality of products; Steel easily are corroded, and the pollutent of Chan Shenging has serious contamination to ion exchange resin therefrom, destroy the result of use of ion exchange resin, and equipment volume is big, takes up an area of wide.
In view of above reason, the purpose of this utility model is for a kind of production pure water quality height is provided, and production cost is low, and save energy is safe in utilization, the ion exchange pure water treater that the life-span is long.
The purpose of this utility model is achieved in that base in the utility model, place the cationic exchange coloum on the base, anion-exchange column, the millipore filter that contains original water inlet valve and wash water valve, the ultra filtration filter that contains the discharge of bacteria valve, the water intaking valve that communicates with cationic exchange is arranged on the base, acid inlet valve, the alkali-feeding valve that communicates with anion-exchange column, outlet, place in the base interchange valve (13) respectively with the entrance end of cationic exchange coloum, the exit end of millipore filter is communicated with, interchange valve (14,16) be connected to cationic exchange coloum by on the mouth end, the entrance end of interchange valve (15) and cationic exchange coloum, the exit end of millipore filter is communicated with, the exit end of interchange valve (17) and cationic exchange coloum, the entrance end of anion-exchange column is communicated with, interchange valve (18) is connected in the entrance end of anion-exchange column, interchange valve (19) is connected to the entrance end of ultra filtration filter, place in the base pipeline with each valve respectively with cationic exchange coloum, anion-exchange column, millipore filter, ultra filtration filter and outlet are communicated with (referring to Fig. 1～Figure 15).
Cross water cap flange on the mounting flange that contains water hole that the tubing string that can adorn the positive and negative resin respectively that contains into and out of the resin mouth is arranged in above-mentioned cationic exchange coloum, the anion-exchange column, is loaded on tubing string top, be fixed on the end socket (referring to Fig. 2) at tubing string top, dress ion exchange resin can adsorb impurity in the exchanged water in tubing string.
Above-mentioned millipore filter; the cylinder that is connected with base is arranged in the ultra filtration filter; be loaded on the filtering membrane platen that pillar stiffener is arranged on the cylinder of being fixed in the cylinder; the filtering membrane platen of the no pillar stiffener that is connected with the filtering membrane platen that pillar stiffener is arranged; the filtering membrane that contains micropore or ultrafiltration hole places the filtering membrane platen and the no supporting seat filtering membrane platen (referring to Fig. 3) of pillar stiffener; place the intravital filtering membrane of post can select for use domestic most advanced ultrafiltration material to make; physical property impurity in the energy filtered water; the energy killing pathogenic bacteria; at any time blowdown can be protected ion exchange column and ion exchange resin.
Above-mentioned cationic exchange coloum, anion-exchange column adopts seamless plexi-glass tubular to make, millipore filter, microfilter adopts synthetic glass to make (referring to Fig. 2, Fig. 3), sun, anion-exchange column adopts seamless plexi-glass tubular to make, the transparency height, but the current intelligence of effective monitoring water treatment procedure intermediate ion exchange resin and water, overcome channeling and the generation of no water subfill phenomenon, in time get rid of the inhibition of CO2 to ion-exchange, guarantee the production of high quality water quality, plexi-glass tubular splendid attire ion exchange resin is pollution-free fully to resin, guarantee the exchange interaction effect and the work-ing life of resin, millipore filter and ultra filtration filter adopt synthetic glass to make, transparency height, but effective monitoring water filtration situation.
Referring to Fig. 1, Fig. 4～Figure 15, pending water through strainer pre-treatment get rid of fully to enter behind the physical property impurity and carry out in the ion exchange column handling degerming through the ultra filtration filter again after chemical treatment is got rid of impurity atom and produced harmless particle and ionic water.Current through technological process are: utilize tap water pressure or pumping pressure (non-tap water feedwater) water to enter the strainer pre-treatment, enter the exchange column chemical treatment again and enter water box after the ultrafiltration again and become high-purity water.
When carrying out chemical treatment, ion exchange resin is introduced (regeneration) harmless ion earlier, during work the introduction resin of the harmful ion in the water is exchanged out harmless ion and enters in the water, produces harmless ionized water thus.After harmful ion filled up resin, resin lost efficacy, and introduced harmless ion by method of reproduction again and entered resin, recovered the function of exchange of resin.
Compare with existing technology, the utlity model has following advantage:
1, the pure water quality height of production, production remove calcium, magnesium ion water, calcium, magnesium ion content are in 0～0.03mmol/L scope, various low pressure boilers are safe and reliable.
2, pure water of producing and high purity water electric conductivity are fit to unit and department's water of any rank water in 0＜1 μ s/cm scope.
3, but direct production, reduce cost so can save a large amount of energy and equipment far above the high purity water of distilled water quality, can be the user and improve the quality of products, reduce the impurity that brings because of water in the product.
4, volume is little, and is in light weight, and floor space is little, and good looking appearance, novelty are easy for operation, antiacid, the caustic corrosion of equipment, long service life.
5, applied widely, can be weight industrial sector, R﹠D institution the novel advanced equipment of producing pure water, high purity water is provided, improve the quality of products; For the low pressure boiler user provides stove outer water treating equipment, prevent that the boiler knot from scaling, prolonged boiler work-ing life, save energy, fund; Can be department such as medicine provides high-quality distilled water to produce product, and fuel economy is economized on the use of funds; Can be urban and rural residents the advanced reliable apparatus of handling polluted source is provided, drink high-cleanness, high water.
Describe embodiment of the present utility model in detail below in conjunction with accompanying drawing:
Fig. 1 is a structural representation of the present utility model.
Fig. 2 is the ion exchange column structural representation.
Fig. 3 is a filter structure schematic representation.
Fig. 4 is inefficacy Zeo-karb counter-flushing process figure.
Fig. 5 is the Zeo-karb into sour schema of regenerating.
Fig. 6 soaks CO for Zeo-karb regeneration
2Schema.
Fig. 7 is for cleaning the Zeo-karb schema.
Fig. 8 is inefficacy anionite-exchange resin counter-flushing process figure.
Fig. 9 is the Zeo-karb into alkali schema of regenerating.
Figure 10 soaks schema for anionite-exchange resin regeneration.
Figure 11 cleans (the fixed bed production recirculated cooling water of holding concurrently) schema for anionite-exchange resin.
Figure 12 is floating bed production cycle cooling water flow path figure.
Figure 13 is fixed bed production store battery water, high-quality distilled water, high-quality pure water schema.
Figure 14 is the blowdown schema.
Figure 15 is the discharge of bacteria schema.
Referring to Fig. 1, the cabinet base 1 that adopts PVC sheet material and chromium steel to be welded is arranged in the utility model, the cationic exchange coloum 2 that is threaded with plate face on the base 1, anion-exchange column 3, the millipore filter 6 that contains original water inlet valve 4 and wash water valve 5, the ultra filtration filter 8 that contains discharge of bacteria valve 7, the water intaking valve 9 that communicates with cationic exchange coloum is arranged on the base 1, acid inlet valve 10, the alkali-feeding valve 11 that communicates with anion-exchange column, outlet 12,21, place in the base interchange valve 13 respectively with the entrance end of cationic exchange coloum, the exit end of millipore filter is communicated with, interchange valve 14,16 are connected on the exit end of cationic exchange coloum, the entrance end of interchange valve 15 and cationic exchange coloum, the exit end of millipore filter is communicated with, the exit end of interchange valve 17 and cationic exchange coloum, the entrance end of anion-exchange column is communicated with, and interchange valve 18 is connected in the entrance end of anion-exchange column, and interchange valve 19 is connected to the entrance end of ultra filtration filter.Place the pipeline 20 in the base that each valve is communicated with cationic exchange coloum, anion-exchange column, millipore filter and ultra filtration filter and outlet respectively. Outlet valve 32,33 is arranged in the exit.
Referring to Fig. 2, cationic exchange coloum, have in the anion-exchange column and adopt the tubing string 23 that contains into and out of resin mouth 22 that has that seamless plexi-glass tubular makes, be loaded on and cross water cap flange 26 on the mounting flange that contains water hole 24 25 on tubing string top, be fixed on the end socket 27 at tubing string top.
Referring to Fig. 3, millipore filter, the cylinder that is connected with base 28 that adopts synthetic glass to make is arranged in the ultra filtration filter, be loaded on the filtering membrane platen 29 that pillar stiffener is arranged on the cylinder of being fixed in the cylinder, with the no pillar stiffener filtering membrane platen 30 that has the supporting seat platen to be connected, the filtering membrane 31 that contains micropore (aperture 0.2～1.0 μ m) or ultramicropore (aperture is less than 20nm) is arranged in two platens 29,30.
Fig. 4 is inefficacy Zeo-karb counter-flushing process figure.Fig. 8 is inefficacy anionite-exchange resin counter-flushing process figure.The utility model is because of by after the long ion-exchange, resin layer in the exchange column has been pressed very tightly, for the resin that makes sphere-like fully loosening, when the step is regenerated exhausted resin down, can fully regenerate, so behind the thoroughly loosening resin layer of recoil resin, can allow regenerator and resin fully act on by Fig. 4, flow process shown in Figure 8.
Fig. 5 is the Zeo-karb into sour schema of regenerating.Resin began to lose efficacy after exchange for some time, last complete failure.Resin loses exchange capacity, at this moment exhausted resin is regenerated with regenerator hydrochloric acid with regard to needing, and recovers the normal exchange capacity of resin, so adopt flow process shown in Figure 5 to make cationic exchange coloum advance acid.
Fig. 6 soaks row CO for Zeo-karb regeneration
2Schema.In hydrochloric acid solution advances cationic exchange coloum, just turn off after resin layer all flooded.Allow proper concn hydrochloric acid solution fully with resin chemistry exchange interaction, make resin recover exchange capacity fully, this process is exactly a regenerative process.The CO that is discharged in the regenerative process
2Gas promptly is excluded in outside the utility model by this process.
Fig. 7 is for cleaning the Zeo-karb schema.After the resin regeneration, harmful ion that is exchanged in the resin and residue acid solution all remain in the exchange column, at this moment by this flow process harmful ion that bears again and spent acid are washed.
Fig. 9 is the anionite-exchange resin into alkali schema of regenerating.Negatively charged ion is to go regeneration to recover exchange capacity with NaOH, and this flow process is exactly the process of input NaOH to anion-exchange column.
Figure 10 is that schema is soaked in anionite-exchange resin regeneration.The NaOH liquid that enters anion-exchange column floods and stops the valve that NaOH into just turns off NaOH liquid behind the negative resin, this moment NaOH just with negative resin chemical exchange (crying regeneration at this moment).This process produces a small amount of gas.This flow process flows to the outer flow process of equipment for gas in the regeneration.
Figure 11 is anionite-exchange resin cleaning process figure (the fixed bed production recirculated cooling water of holding concurrently).After the negative resin regeneration, to get rid of harmful (in the former water) negatively charged ion in the resin, as Cl
-1, SO
4 -2Deng, at this moment the surplus NaOH that has not regenerated in addition will wash in addition.Clean negatively charged ion and must spend again, so must clean anion-exchange column with the water that the cleaned resin of cationic exchange coloum goes out except cationic softening water cleaning.Shown in Figure 11 is exactly anion-exchange column behind the cleaning and regeneration.
Figure 12 is floating bed production cycle cooling water flow path figure.After the positive and negative resin regeneration was good, cleaned, the positive and negative resin had all recovered exchange capacity, at this moment just produced water (promptly removing the positive and negative ion in the feedwater).Figure 12 promptly is the process of reverse-flow production water.
Figure 13 is fixed bed store battery water, high-quality distilled water, high-quality pure water schema.This flow process is that the three grades of pure water (rudimentary pure water) that exchanged are once produced sterilized water through the ultra filtration filter.
Figure 14 is the blowdown schema.This flow process is that be not visible to the physical eyes on the filtering membrane in the strainer (aperture is between 0.2 μ m～1 μ m) precipitation, suspended substance being etc. are got rid of at any time.
Figure 15 is the discharge of bacteria schema.This flow process is to kill with formaldehyde after being rejected to the multiple thalline that the retaining of ultra filtration filter membrane (aperture is less than the 20nm) top in the ultra filtration filter has in the pond at any time.
Arrow among Fig. 4～Figure 15 is represented flow line.
Claims (4)
1, the ion exchange pure water treater, it is characterized in that base (1) is arranged in the described treater, place the cationic exchange coloum (2) on the base, anion-exchange column (3), the millipore filter (6) that contains original water inlet valve (4) and wash water valve (5), the ultra filtration filter (8) that contains discharge of bacteria valve (7), base (1) is provided with the water intaking valve (9) that communicates with cationic exchange coloum, acid inlet valve (10), the alkali-feeding valve that communicates with anion-exchange column (11), outlet (12,21), place in the base interchange valve (13) respectively with the entrance end of cationic exchange coloum, the exit end of millipore filter is communicated with, interchange valve (14,16) be connected on the exit end of cationic exchange coloum, the entrance end of interchange valve (15) and cationic exchange coloum, the exit end of millipore filter is communicated with, the exit end of interchange valve (17) and cationic exchange coloum, the entrance end of anion-exchange column is communicated with, interchange valve (18) is connected in the entrance end of anion-exchange column, interchange valve (19) is connected to the entrance end of ultra filtration filter, place in the base pipeline with each valve respectively with cationic exchange coloum, anion-exchange column, millipore filter and ultra filtration filter and outlet are communicated with.
2, ion exchange pure water treater as claimed in claim 1, it is characterized in that having in described cationic exchange coloum, the anion-exchange column tubing string that can adorn the positive and negative resin respectively that contains into and out of the resin mouth, be loaded on and cross water cap flange on the mounting flange that contains water hole on tubing string top, be fixed on the end socket at tubing string top.
3, ion exchange pure water treater as claimed in claim 1, it is characterized in that in described millipore filter, the ultra filtration filter cylinder that is connected with base being arranged, be loaded on the filtering membrane platen that pillar stiffener is arranged on the cylinder of being fixed in the cylinder, the no pillar stiffener filtering membrane platen that is connected with the filtering membrane platen that pillar stiffener is arranged, the filtering membrane that contains micropore or ultrafiltration hole places the filtering membrane platen and the no pillar stiffener filtering membrane platen of pillar stiffener.
4, ion exchange pure water treater as claimed in claim 1 is characterized in that described cationic exchange coloum, anion-exchange column adopt seamless plexi-glass tubular to make, and millipore filter, ultra filtration filter adopt synthetic glass to make.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96224290 CN2277985Y (en) | 1996-12-30 | 1996-12-30 | Ion exchanging pure water treating device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96224290 CN2277985Y (en) | 1996-12-30 | 1996-12-30 | Ion exchanging pure water treating device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2277985Y true CN2277985Y (en) | 1998-04-08 |
Family
ID=33903315
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 96224290 Expired - Fee Related CN2277985Y (en) | 1996-12-30 | 1996-12-30 | Ion exchanging pure water treating device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2277985Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100447957C (en) * | 2001-10-31 | 2008-12-31 | 株式会社日立制作所 | Manufacture of semiconductor integrated circuit device |
| WO2016065546A1 (en) * | 2014-10-29 | 2016-05-06 | Dow Global Technologies Llc | Water treatment assembly including hyperfiltration module and cation exchange resin |
-
1996
- 1996-12-30 CN CN 96224290 patent/CN2277985Y/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100447957C (en) * | 2001-10-31 | 2008-12-31 | 株式会社日立制作所 | Manufacture of semiconductor integrated circuit device |
| WO2016065546A1 (en) * | 2014-10-29 | 2016-05-06 | Dow Global Technologies Llc | Water treatment assembly including hyperfiltration module and cation exchange resin |
| US10040704B2 (en) | 2014-10-29 | 2018-08-07 | Dow Global Technologies Llc | Water treatment assembly including hyperfiltration module and cation exchange resin |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |