CN115025824B - Ion exchanger - Google Patents
Ion exchanger Download PDFInfo
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- CN115025824B CN115025824B CN202210568943.9A CN202210568943A CN115025824B CN 115025824 B CN115025824 B CN 115025824B CN 202210568943 A CN202210568943 A CN 202210568943A CN 115025824 B CN115025824 B CN 115025824B
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- Prior art keywords
- distributor
- shell
- ion exchanger
- bottom plate
- top plate
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- 150000002500 ions Chemical class 0.000 claims description 96
- 239000011347 resin Substances 0.000 claims description 66
- 229920005989 resin Polymers 0.000 claims description 66
- 230000008929 regeneration Effects 0.000 claims description 28
- 238000011069 regeneration method Methods 0.000 claims description 28
- 239000000463 material Substances 0.000 claims description 26
- 238000013461 design Methods 0.000 claims description 19
- 239000002245 particle Substances 0.000 claims description 17
- 238000000034 method Methods 0.000 claims description 15
- 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 description 9
- 238000009826 distribution Methods 0.000 claims description 9
- 238000004804 winding Methods 0.000 claims description 9
- 239000011324 bead Substances 0.000 claims description 8
- 239000002253 acid Substances 0.000 claims description 7
- 238000005260 corrosion Methods 0.000 claims description 7
- 239000003456 ion exchange resin Substances 0.000 claims description 7
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 7
- 230000007797 corrosion Effects 0.000 claims description 6
- 238000005253 cladding Methods 0.000 claims description 5
- 230000005484 gravity Effects 0.000 claims description 5
- 239000007769 metal material Substances 0.000 claims description 5
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 4
- 239000004063 acid-resistant material Substances 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 4
- 238000005349 anion exchange Methods 0.000 claims description 4
- 238000005341 cation exchange Methods 0.000 claims description 4
- 239000000919 ceramic Substances 0.000 claims description 4
- 229920001971 elastomer Polymers 0.000 claims description 4
- 230000009972 noncorrosive effect Effects 0.000 claims description 4
- 239000011148 porous material Substances 0.000 claims description 4
- 239000010936 titanium Substances 0.000 claims description 4
- 229910052719 titanium Inorganic materials 0.000 claims description 4
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 3
- 229910001018 Cast iron Inorganic materials 0.000 claims description 3
- 229910045601 alloy Inorganic materials 0.000 claims description 3
- 239000000956 alloy Substances 0.000 claims description 3
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 claims description 3
- 239000003830 anthracite Substances 0.000 claims description 3
- 239000010962 carbon steel Substances 0.000 claims description 3
- 239000011521 glass Substances 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 230000000712 assembly Effects 0.000 claims description 2
- 238000000429 assembly Methods 0.000 claims description 2
- 239000004033 plastic Substances 0.000 claims description 2
- 239000012492 regenerant Substances 0.000 abstract description 40
- 239000010865 sewage Substances 0.000 abstract description 8
- 238000009776 industrial production Methods 0.000 abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- 230000000694 effects Effects 0.000 description 18
- 239000002699 waste material Substances 0.000 description 15
- 238000005342 ion exchange Methods 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 11
- 238000000746 purification Methods 0.000 description 10
- 238000007789 sealing Methods 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000003957 anion exchange resin Substances 0.000 description 7
- 239000007864 aqueous solution Substances 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- FBPFZTCFMRRESA-KVTDHHQDSA-N D-Mannitol Chemical compound OC[C@@H](O)[C@@H](O)[C@H](O)[C@H](O)CO FBPFZTCFMRRESA-KVTDHHQDSA-N 0.000 description 4
- 229930195725 Mannitol Natural products 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000001514 detection method Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000000594 mannitol Substances 0.000 description 4
- 235000010355 mannitol Nutrition 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
- 150000001450 anions Chemical class 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 3
- 239000003729 cation exchange resin Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 235000013305 food Nutrition 0.000 description 3
- 230000007935 neutral effect Effects 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 238000003466 welding Methods 0.000 description 3
- LFTLOKWAGJYHHR-UHFFFAOYSA-N N-methylmorpholine N-oxide Chemical compound CN1(=O)CCOCC1 LFTLOKWAGJYHHR-UHFFFAOYSA-N 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 230000004075 alteration Effects 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 238000012790 confirmation Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- -1 when in use Substances 0.000 description 2
- SAPGTCDSBGMXCD-UHFFFAOYSA-N (2-chlorophenyl)-(4-fluorophenyl)-pyrimidin-5-ylmethanol Chemical compound C=1N=CN=CC=1C(C=1C(=CC=CC=1)Cl)(O)C1=CC=C(F)C=C1 SAPGTCDSBGMXCD-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 244000043261 Hevea brasiliensis Species 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 229920000433 Lyocell Polymers 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 239000006004 Quartz sand Substances 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000002421 anti-septic effect Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 235000013365 dairy product Nutrition 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 229920003052 natural elastomer Polymers 0.000 description 1
- 229920001194 natural rubber Polymers 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention discloses an ion exchanger, and belongs to the technical field of purifying equipment. The device comprises a shell, an upper top plate, a lower bottom plate, a pull stay bar, an upper distributor, a lower distributor and a filling layer, wherein the upper top plate and the lower bottom plate are respectively arranged on the upper side and the lower side of the shell along the radial direction, a containing space is formed inside the enclosure of the shell, the upper top plate and the lower bottom plate, and the pull stay bar is supported between the upper distributor and the lower distributor; the upper distributor passes through one side of the shell and is fixedly connected with part or all of the pull stay bars, and an inlet pipe of the upper distributor is formed at one side of the upper distributor; the lower distributor passes through one side of the shell and is fixedly connected with part or all of the pull stay bars, and an inlet pipe of the lower distributor is formed at one side of the lower distributor; the filling layer is arranged above the lower bottom plate, and the filling height of the filling layer is higher than the upper horizontal tangent line of the lower distributor. It is suitable for large-scale industrial production, and can save regenerant and reduce sewage generation.
Description
Technical Field
The invention relates to the technical field of purifying equipment, in particular to an ion exchanger.
Background
The ion exchange method is a method of exchanging a solid phase exchanger containing an ion and an ion in a solution. The method has the advantages of strong selectivity and high concentration multiple as a unique separation technology, and is applied to multiple fields in multiple industries. Ion exchange reactions are the exchange between ions, i.e., one ion in solution is adsorbed onto the exchanger while replacing an equivalent of the same type of ion. Ion exchangers are a type of reaction bed for carrying out ion exchange reactions, and need to have two functions: exchange and regeneration. The exchange is to pass the material to be purified through an ion exchanger, and the ions which are not needed in the material are exchanged with the ions which are needed on the exchange resin. The regeneration is to exchange the needed ions with the unnecessary ions fully adsorbed by the resin by using a regenerant after the ion exchange resin is saturated in adsorption, so that the resin can be reused. According to the above, the ion exchanger always has two processes of exchange and regeneration circulating.
Disclosure of Invention
In view of this, the present invention provides an ion exchanger which is suitable for large-scale industrial production and can save regenerant and reduce sewage generation, thereby being more practical.
In order to achieve the first object, the technical scheme of the ion exchanger provided by the invention is as follows:
the invention provides an ion exchanger, which comprises a shell (1), an upper top plate (2), a lower bottom plate (3), a pull stay bar (4), an upper distributor (6), a lower distributor (7) and a filling layer (5),
The upper top plate (2) and the lower bottom plate (3) are respectively arranged on the upper side and the lower side of the shell (1) along the radial direction, and a containing space is formed in the interior surrounded by the shell (1), the upper top plate (2) and the lower bottom plate (3)'
The pull stay bar (4) is supported between the upper distributor (6) and the lower distributor (7);
The upper distributor (6) passes through one side of the shell (1) and is fixedly connected with part or all of the pull stay bars (4), and an inlet pipe of the upper distributor (6) is formed at one side of the upper distributor (6);
The lower distributor (7) passes through one side of the shell (1) and is fixedly connected with part or all of the pull stay bars (4), and an inlet pipe of the lower distributor (7) is formed at one side of the lower distributor (7);
The filling layer (5) is arranged above the lower bottom plate (3), and the filling height of the filling layer (5) is higher than the upper horizontal tangent line of the lower distributor (7).
The ion exchanger provided by the invention can be further realized by adopting the following technical measures.
Preferably, the ion exchanger is applied to anion exchange or cation exchange, and the material for manufacturing the ion exchanger is selected according to two application working conditions.
Preferably, the shell is made of a metal material, wherein the metal material is selected from one of carbon steel, stainless steel, metallic titanium and cast iron alloy, the diameter is more than or equal to 1.5m, the height is more than or equal to 1.5m, the wall thickness is more than or equal to the calculated thickness of +2mm, and the shell is required to be subjected to corrosion-resistant rubber lining treatment when being contacted with a corrosive medium.
Preferably, the material of the pull stay bar (4) is the same as that of the shell (1), and the pull stay bar is welded between the upper top plate (2) and the lower bottom plate (3), so that the pull stay bar is required to be subjected to corrosion-resistant rubber lining treatment when contacting corrosive media.
Preferably, the stay bars (4) are uniformly distributed in the accommodating space, the number of the stay bars is determined according to the diameter of the shell and the design pressure, the distance between the stay bars (4) and the shell (1) and the distance between two adjacent stay bars (4) are furthest less than 30 times of the diameter of the stay bars (4), and the number of the stay bars is a positive integer which is more than or equal to 1.
Preferably, the cross-sectional area of the single stay bar (4) is calculated according to the following formula:
a, drawing the sectional area of a stay bar, and mm 2;
w is the axial load of a single pull stay rod, N;
[ Sigma ] -allowable stress of stay rod material at design temperature, MPa
Preferably, the upper top plate (2) and the lower bottom plate (3) are of flat plate structures, are the same in material and material as the shell (1), are welded with the shell (1), and are required to be subjected to corrosion-resistant rubber lining treatment when being contacted with corrosive media.
Preferably, the upper top plate (2) and the lower bottom plate (3) are provided with holes which are the same in number and positions as the pull stay bars (4), and the pull stay bars penetrate through the holes and are welded with the upper top plate (2) and the lower bottom plate (3).
Preferably, the thicknesses of the upper top plate (2) and the lower bottom plate (3) are calculated according to the following formula:
Delta-thickness of the upper top plate (2) and the lower bottom plate (3), mm;
L is the distance between the pull stay bars (4) and the shell (1), and the farthest distance between two adjacent pull stay bars (4) is mm;
Pc-design pressure, MPa;
[ sigma ] -allowable stress of the material of the bottom plate (3) at the design temperature, MPa;
K, the connection method coefficient of the upper top plate (2) and the lower bottom plate (3);
preferably, the lower distributor (7) is positioned above the lower bottom plate (3), and the tangential distance between an inlet pipe of the lower distributor (7) and the lower bottom plate (3) is 0-20 mm;
When the distributor is applied to a non-corrosive medium, the lower distributor (7) is the same as the shell (1), and an inlet pipe of the lower distributor (7) is welded on the shell (1); when the lower distributor (7) needs to be contacted with corrosive media, the lower distributor is made of acid-resistant materials, and is connected and sealed with the shell (1) by a stuffing box.
Preferably, the upper distributor (6) is located below the upper top plate (2), and the tangential distance between the inlet pipe of the upper distributor (6) and the upper top plate (2) is calculated according to the following formula:
H＝HL×0.18+200
h, the tangential distance between the upper distributor (6) and the upper top plate (2) is mm;
HL, height of the shell (1), mm;
When the distributor is applied to a non-corrosive medium, the material of the upper distributor (6) is the same as that of the shell (1), and an inlet pipe of the upper distributor (6) is welded on the shell (1); when the upper distributor (6) needs to be contacted with corrosive media, the upper distributor is made of acid-resistant materials, and is connected and sealed with the shell (1) by a stuffing box.
Preferably, the lower distributor (7) and the upper distributor (6) adopt calandria type distribution, the calandria comprises linear calandria or circular calandria, preferably circular calandria, the calandria adopts one or more modes of micro-pore pipe, macro-pore pipe cladding gauze and wire winding pipe, preferably wire winding pipe mode, the gap of each calandria pipe is selected to be between 0.15mm and 0.2mm, according to the maximum flow rate of exchange or regeneration, the discharge flow rates of the upper distributor (6) and the lower distributor (7) into the accommodating space are selected to be between 0.05m/s and 0.1m/s, and the total flow rate of the distributor is selected to be between 1m/s and 1.5m/s.
Preferably, the filling layer (5) is one or more of anthracite particles, ceramic beads, glass beads and plastic beads with acid and alkali resistance, preferably ceramic beads, the specific gravity of the filling particles is more than or equal to 1.5g/cm 3, and the particle size is selected from microporous apertures, coated net meshes and wire winding pipe gaps which are 5-10 times of the particle size.
Preferably, the ion exchanger is further provided with one or more conventional container assemblies of a manhole, a hand hole, a safety valve, an exhaust hole and a window.
Preferably, the ion exchanger is used for filling chlorine type ion exchange resin to the central line of the upper distributor (6) during anion exchange and filling sodium type ion exchange resin to the central line of the upper distributor (6) during cation exchange.
As can be seen from the above manufacturing method, the ion exchanger provided by the invention is different from the conventional technology in three main aspects:
The method comprises the following steps: the invention gets rid of the dependence of the conventional technology on the upper and lower seal heads, and replaces two flat plates, so that 25% -30% of regenerant can be saved, but the problem of easy deformation of the flat plate structure is brought, and the invention develops a stretching structure and a welding combination mode which are suitable for the stress of the flat plates to solve the problem, so that the ion exchanger can bear the stress in the exchange process.
And two,: the invention solves the problem of internal distribution of a large ion exchanger, besides designing a special distributor, the invention utilizes a filling layer to isolate resin from the distributor for secondary distribution, solves the problems of uneven distribution, broken resin, dusai water caps and the like of the conventional ion exchanger, and improves the utilization rate of the resin and the exchange effect.
And thirdly,: the invention is suitable for large-scale ion exchangers, and solves the problem that a large-scale engineering needs a plurality of parallel sets because of small size of the conventional ion exchangers.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to designate like parts throughout the figures. In the drawings:
FIG. 1 shows a schematic diagram of an ion exchanger according to an embodiment of the present invention;
Fig. 2 shows a schematic structural diagram of a linear calandria distributor used in an ion exchanger according to an embodiment of the present invention;
FIG. 3 shows a schematic view of a circular gauntlet distributor for ion exchanger applications provided by an embodiment of the present invention;
fig. 4 is a schematic plan view showing an arrangement manner of pull rods used in the ion exchanger according to the embodiment of the present invention when the pull rods are arranged in a regular triangle.
Detailed Description
In view of this, the present invention provides an ion exchanger which is suitable for large-scale industrial production and can save regenerant and reduce sewage generation, thereby being more practical.
The inventor has made hard observations and has found that, after the ion exchange process is established, the user generally has two desires, namely, to improve the ion exchange effect and to save regenerant.
Improving the ion exchange effect is sought after by most users, for example, in the energy and power industry, improving the ion exchange effect means that the service life of boilers and power generation equipment is longer and the efficiency is higher, and in the propylene glycol purification field, improving the ion exchange effect means that the product purity is high and the application field is wider; improving the ion exchange effect in the field of dairy products means that the food has lower heavy metal ions and safer food.
The cost and emission reduction of the regenerant are required. The regenerant is required to provide the ions required for purification to the resin and replace the harmful ions saturated by adsorption on the resin. Typically acids, bases and salts, when acids are used as regenerants, H + ions are provided to the resin to replace lower metal ions and cations, and the regenerated waste liquid needs to be neutralized with bases; when regenerated with alkali, OH - ions are provided to the resin to replace the lower anions, and the regenerated waste liquid needs to be neutralized with acid; when regenerating with salt, it is necessary to select the salt according to the ions required for the purification liquid. Saving regenerant means reducing regenerant costs and reducing sewage costs.
The traditional manufacturing method of industrial ion exchanger adopts a container containing upper and lower elliptical sealing heads as main body structure, a branch pipe capable of discharging waste regenerant, when in use, resin with about 50% of equipment capacity is filled, quartz stone and quartz sand with certain thickness are placed on the lower sealing heads of the early ion exchanger to be used as filter materials for bearing resin, and as resin is lost frequently, the manufacturing mode is eliminated gradually, and a filter plate for bearing resin is used instead, so that the problem of resin loss is solved. Such techniques mainly involve the following four drawbacks:
Firstly, there is no special distributor during exchange and regeneration, for large-diameter ion exchangers, the exchange liquid or regenerant can permeate through the path with minimum resistance, namely, the central permeation quantity of the ion exchanger is more, the peripheral permeation quantity is less, so that the resin utilization rate during exchange is low, the resin regeneration effect during regeneration is different, and the use effect is affected.
Secondly, in order to ensure the exchange quality, most ion exchange processes select countercurrent regeneration, namely, the regenerant enters the ion exchanger from bottom to top, and due to structural limitation, when the regeneration is finished, part of new regenerant is left in the seal head and is not contacted with the resin, and the regenerant is discharged as waste acid and alkali without function, so that about 20% of regenerant is wasted, and more 20% of sewage is generated.
Third, at the end of regeneration, in order to remove the regenerated waste regenerant from the upper part of the resin layer, the waste regenerant passes through the resin layer again, and at this time, a part of harmful ions in the waste regenerant returns to the resin to form reverse regeneration.
Fourthly, the ion exchanger is difficult to be made large due to the stress limitation of the material port, the supporting leg and the bearing resin filter plate, and a large-scale water treatment and purification system needs a plurality of identical devices to operate.
From the above description, it is known that developing a large-sized, economical and efficient ion exchanger can solve the above problems, and achieve the purposes of saving production cost and reducing sewage discharge.
The existing ion exchanger comprises a container with upper and lower elliptical sealing heads as a main structure, and a branch pipe for carrying resin filter plates and discharging waste regenerant is arranged in the container, so that the main defects of the equipment are that the exchange and regeneration are unevenly distributed, the resin utilization rate is low, the efficiency is poor, the larger the equipment filling quantity is, the more serious the phenomenon is, the lower sealing head structure wastes the regenerant, and although the field with low requirement on the exchange result can mix and recycle the new regenerant existing in the lower sealing head with the waste regenerant existing between resin layers, the impurities adsorbed by the resin in the exchanger can not be replaced, and only the impurities in the waste regenerant can be further dispersed in the resin, so that the waste regenerant is more wasted. The last disadvantage is that the structure is difficult to be made large due to the limitation of the stress of the supporting legs, the stress of the lower sealing head and the stress of the resin carrier plate. The inventor of the present invention found that when the regeneration agent is saved by researching the improvement of the large-scale ion exchange effect, the ideal effect is hardly achieved only by adding the distributor, the actual waste is derived from the use of the new regeneration agent and the discharge of the waste regeneration agent by the ion exchanger, and the distributor plays a very important role as a part of improving the use efficiency of the regeneration agent.
In order to further describe the technical means and effects adopted for achieving the preset aim of the present invention, the following description refers to the specific implementation, structure, characteristics and effects of an ion exchanger according to the present invention with reference to the accompanying drawings and preferred embodiments. In the following description, different "an embodiment" or "an embodiment" do not necessarily refer to the same embodiment. Furthermore, the particular features, structures, or characteristics of one or more embodiments may be combined in any suitable manner.
The term "and/or" is herein merely an association relation describing an associated object, meaning that three relations may exist, e.g. a and/or B, specifically understood as: the composition may contain both a and B, and may contain a alone or B alone, and any of the above three cases may be provided.
Referring to fig. 1 to 3, the ion exchanger provided by the invention is composed of the following structures:
A1, the ion exchanger mainly comprises a shell 1, an upper top plate 2, a lower bottom plate 3, a pull stay bar 4, an upper distributor 6, a lower distributor 7 and a filling layer 5;
A2, other parts except the filling layer 5 are connected together in a welding mode or a stuffing box mode;
A3, the filling layer 5 is laid on the lower bottom plate 3 by hand.
The shell 1 is a main body for containing ion exchange resin and supporting equipment and is made of metal materials, wherein the metal materials comprise carbon steel, stainless steel, metallic titanium and cast iron alloy, the diameter is more than or equal to 1.5m, and the height is more than or equal to 1.5m.
Further, since the types of the resins and the materials to be purified are different, the resin stacking shapes required by the process are different, and the filling amount and the length-diameter ratio of the resins required by the process are not within the confirmation range of the invention, the invention only provides the design of the ion exchanger on the premise of knowing the filling amount and the length-diameter ratio.
Further, when the shape of the resin filling layer 5 is determined, first, the diameter of this filling layer 5 is not less than 1.5m, and after this parameter is satisfied, the formula is given: h=hl×0.18+200, hl= (ht+200)/0.82
H, the tangential distance between the upper distributor 6 and the upper top plate 2 is mm;
HL, height of the shell 1, mm;
HT, resin filling height, mm, wherein the ion exchanger is filled with resin when in use, wherein the resin filling height refers to the filling height of the ion exchanger filled with resin when in use;
The height of the housing can be calculated according to the above formula. It should be noted that the present invention differs from the conventional art in terms of the resin filling height, which is half of the height of the straight tub section of the ion exchanger, and it can be simply understood that hl=ht×2, the filling ratio of the present invention is larger.
When the solution penetrates the resin layer, the resin layer generates resistance, namely pressure is needed to ensure a certain flow rate to penetrate the resin layer, so that the internal pressure exists in the exchange process, and the pressure has a great relation with the type of the resin, the materials to be purified and the flow rate and is not in the confirmation range of the invention. The shell needs to bear radial pressure, the thickness of the shell 1 can be calculated according to GB 150-2011, the thickness of the shell 1 needs to be increased by 2mm in order to ensure and distribute the welding of the pipes and the upper top plate 2 and the lower bottom plate 3 and solve the problem of local loss after a period of operation.
The stay bars 4 are used for increasing the stability of the upper top plate 2 and the lower bottom plate 3, are uniformly distributed in the ion exchanger, and mainly satisfy three conditions when the number of the stay bars 4 is determined:
The number is more than or equal to 1;
the number is determined according to the diameter of the shell 1 and the design pressure, and the distance between the stay bar 4 and the shell 1 and the farthest distance (L) between two adjacent stay bars 4 are smaller than 30 times of the diameter (d) of the stay bar 4.
The calculation formula of the sectional area of the single stay bar 4 is as follows:
a, the sectional area of the pull stay bar 4 is mm 2;
W is the axial load of a single pull stay rod 4, N;
[ Sigma ] -allowable stress of pull rod 4 material at design temperature, MPa
Further, the distance between the stay bar 4 and the shell 1 and the furthest distance (L) between two adjacent stay bars 4 determine the load of the stay bar 4, and the most economical way is that the distances between the stay bar 4 and the shell 1 and between two adjacent stay bars 4 are equal.
When designing the pull stay bars 4, the initial number of the pull stay bars 4 is given according to the above conditions, and then the number, the diameter and the arrangement mode of the pull stay bars 4 can be obtained by calculating and performing back calculation, usually 2-3 times of calculation.
After the number of stay bars 4 is determined, the thicknesses of the upper and lower top plates 2 and 3 are calculated as follows:
Delta-thickness of upper top plate 2 and lower bottom plate 3, mm;
L is the distance between the stay bar 4 and the shell 1, and the distance between two adjacent stay bars 4 is the farthest, mm;
Pc-design pressure, MPa;
[ Sigma ] -allowable stress of material at design temperature, MPa; (upper top plate 2 and lower bottom plate 3)
K, the connection method coefficient of the upper top plate 2 and the lower bottom plate 3;
Wherein the K value can be found in GB 150-2011.
The mode of the invention for improving the ion exchange efficiency mainly controls the flowing range of the solution (regenerant) through a lower distributor 6 and an upper distributor 7, wherein the distributors adopt calandria distribution, and calandria can be composed of linear calandria or circular calandria, as shown in figure 3 of figure 2, and is preferably circular calandria. The calandria can be made by three modes of microporous pipe, macroporous pipe cladding gauze and wire winding pipe, and is preferably selected from the wire winding pipe mode. The aperture of the micropore, the mesh of the cladding net and the gaps of the wire winding pipe are selected to be between 0.15 and 0.2mm, the discharge flow rate of the distributor into the ion exchanger is selected to be between 0.05 and 0.1m/s according to the maximum flow rate of exchange or regeneration, and the total flow rate of the distributor is selected to be between 1 and 1.5m/s. When the exchange or regeneration process is determined, the distributor may be determined based on the parameters described above.
After passing through the lower distributor 7, the solution (regenerant) firstly passes through the filling layer 5, the filling layer 5 is composed of a plurality of particles with large particle size, after passing through the filling layer 5, the solution (regenerant) is distributed again and then enters the resin layer, in order to ensure the distribution effect, the specific gravity of the filling particles is more than or equal to 1.5g/cm 3, and the particle size of the filling particles is selected to be 5-10 times of the actual gaps of the distributor.
The ion exchanger is in a high floating state when resin regeneration is not needed, and resin is not needed to move at a high speed to drive a resin layer, so that resin is prevented from being broken.
The manufacture and use of the ion exchanger of the present invention will be further illustrated by the following examples. However, the ion exchanger provided by the present invention is not limited to the solutions mentioned in the following examples, and the aqueous solutions purified by ion exchange resins and ion exchangers in the prior art are suitable for use in the present invention.
Example 1:
Lyocell fibre solvent purification is a representative field of ion exchanger applications, where the solvent to be purified is a 15% to 25% aqueous solution of N-methyl-morpholine oxide, in the nature of an organic amine.
The invention designs and manufactures a large anion exchanger applied to the field, the exchanger can be filled with 0.55mm average particle anion exchange resin 160m 3, the design pressure is 0.6MPa, the appearance of the resin layer is phi 5500 multiplied by 6800, and S304 is selected as a manufacturing material.
The length of the housing 1 is calculated according to the formula hl= (ht+200)/0.82, hl=8537 mm. Shell 1 thickness = calculated thickness +2mm, calculated thickness based on internal pressure vessel, calculated thickness 14.2mm, shell 1 thickness 16.2mm.
The stay bars are arranged in a regular triangle shape, 19 stay bars are taken, and the formula is adoptedThe diameter of the pull stay bar 4 is between 64mm and 77mm, the diameter of the pull stay bar 4 is 70mm, the farthest distance between the adjacent pull stay bars 4 is 917mm, and the diameter of the adjacent pull stay bar 4 is less than 30 times of the diameter of the pull stay bar 4.
The thickness of the upper top plate 2 and the lower bottom plate 3 is calculated according to the formula41Mm was calculated.
And manufacturing an upper distributor 6 and a lower distributor 7 according to a schematic diagram 3, wherein the distributors are made of S304 distributor materials, the branch pipes are made of metal wire winding pipes, and the upper distributor 6 and the lower distributor 7 are welded on the shell 1 of the ion exchanger.
After the ion exchanger is manufactured and installed according to the conditions, ceramic sand with the specific gravity of more than or equal to 2.2g/cm < 3 > and 1.5mm is paved on the lower bottom plate 3 and is paved on the lower distributor 7.
When in use, the uniform particle type anion exchange resin with the thickness of 0.55mm is filled to the horizontal tangent line on the upper distributor 6, the filling amount is about 160m 3, the resin is regenerated by 336m 3 4.5.5 percent sodium hydroxide (2.1 times of the bed volume), then the resin is washed to be neutral in outflow water, the resin is used for purifying 15 percent of N-methyl-morpholine oxide aqueous solution, the chromaticity after purification is less than or equal to 10PCU, the conductivity is 5 mu s/cm, and the purification bed volume reaches 300BV and then is saturated and regenerated.
The conductivity detection method comprises the following steps: on-line conductivity meter
The chromaticity detection method comprises the following steps: on-line colorimeter
In the embodiment, the manufactured ion exchanger is filled with 160m 3 of anion exchange resin, and the conventional equipment can be maximally 30m 3 due to the limitation of the stress of the resin bearing plate and the sealing head, and can be completed only by using 6 conventional ion exchangers in the embodiment 1. In the embodiment, 4.5% sodium hydroxide with 2.1 times of bed volume is adopted as the regenerant to regenerate the resin, and a conventional exchanger generally adopts 4.5% sodium hydroxide with 3 times of bed volume to regenerate the resin, but the actual regenerant contacting the resin is only 2.4 bed volumes, the conductivity reaches 5 mu s/cm after being used for purifying sewage, the conductivity is superior to the conventional 10 mu s/cm, the volume of the exchange bed can reach 300 and is 7% higher than the volume of a conventional 280 bed, so that the regeneration and exchange effect of the embodiment is superior to the conventional technology, and 30% of regenerant is saved.
Example 2:
The invention designs and makes a large-scale cation exchanger applied to the field, the exchanger can be filled with 0.65mm uniform particle cation exchange resin 60m 3, the design pressure is 0.4MPa, the appearance of the resin layer is phi 4000 x 4800, Q235B is selected as a main material, and natural rubber is lined for antiseptic treatment.
The housing 1 length is calculated according to the formula hl= (ht+200)/0.82, hl=6098 mm. The thickness of the shell 1 = calculated thickness +2mm, the calculated thickness is calculated according to the internal pressure container, the calculated thickness is 8.4mm, the thickness of the shell 1 is 10.4mm, and the steel plate with the nominal thickness of 12mm can be selected for manufacturing.
The stay bars 4 are arranged in a regular triangle shape, 7 stay bars are taken, and the formula is adoptedThe diameter of the pull stay rod is between 62mm and 75mm, the diameter of the pull stay rod 4 is 65mm, the farthest distance between the adjacent pull stay rods 4 is 1000mm, and the diameter of the pull stay rod 4 is less than 30 times of the diameter of the pull stay rod.
The thickness of the upper top plate 2 and the lower bottom plate 3 is calculated according to the formulaCalculated 40mm.
And adding conventional container accessories such as a manhole, an exhaust hole, a safety valve hole and the like on the basis of the main body data, and then lining with anti-corrosion acid-resistant glue, wherein the manhole is a device for entering people during container maintenance.
The upper distributor 6 and the lower distributor 7 are manufactured according to a schematic diagram 2, the distributors are made of titanium tubes as supporting materials, a plurality of holes with the diameter of 20mm are formed in a branch tube, a polypropylene filter screen with the aperture of 0.15mm is used for coating, the branch tube is connected with an ion exchanger main body through a stuffing box, and the distributors are fixed and kept sealed.
After the ion exchanger is installed, 2mm glass beads are spread on the lower plate 3 and spread on the lower distributor 7.
When in use, the uniform particle type cation exchange resin with the filling amount of 0.65mm is filled to the horizontal tangent line on the upper distributor, the filling amount is about 60m 3, 135m35 percent hydrochloric acid (2.25 times of the bed volume) is used for regeneration, washing is carried out until the effluent water is neutral, the water is used for purifying the water which passes through the anion exchange resin, the conductivity reaches 0.75 mu s/cm after the water exchange, and the purified bed volume reaches 16000BV, and the regeneration treatment is carried out after the conductivity reaches 1 mu s/cm.
The detection method comprises the following steps: an on-line conductivity meter.
In the embodiment, the manufactured ion exchanger is filled with cation exchange resin of 60m 3, and the conventional equipment can be maximally 30m 3 due to the stress limitation of the resin bearing plate and the sealing head, and can be completed only by the aid of the embodiment 1 under the condition that two conventional ion exchangers are needed. In the embodiment, the 5% hydrochloric acid with the volume of 2.25 times of the bed volume is adopted as the regenerant to regenerate the resin, and the conventional exchanger generally adopts the 5% hydrochloric acid with the volume of 3 times of the bed volume, but the regenerant actually contacting the resin is only 2.4 bed volumes, and the conductivity reaches 0.75 mu s/cm after being used for purifying sewage, which is superior to the conventional one with the volume of 1 mu s/cm and the bed volume of 16000BV and superior to the conventional one with the volume of 15000BV, so that the regeneration and exchange effect of the embodiment is not lower than that of the conventional technology, and 25% of regenerant is saved.
Example 3:
The food purification is a brand new field of the application of the ion exchanger, the substance to be purified is mannitol aqueous solution, and macroporous anion exchange resin is adopted to purify the mannitol aqueous solution.
The invention designs and manufactures a medium-sized anion exchanger which can be filled with macroporous anion exchange resin 4.8m 3 with the thickness of 0.35 mm-0.85 mm, the design pressure is 0.5MPa, the appearance of a resin layer is phi 1600 multiplied by 2400, and S316L is selected as a manufacturing material.
The shell length is calculated according to the formula hl= (ht+200)/0.82, hl=2644 mm. Shell thickness = calculated thickness +2mm, calculated thickness calculated from the internal pressure vessel, calculated thickness 4.0mm, shell thickness 6.0mm.
The number of the pull stay bars is1, and the formula is based onThe diameter of the pull stay rod is between 55mm and 66mm, the diameter of the pull stay rod is 60mm, the distance between the pull stay rod and the outer wall is 800mm, and the diameter of the pull stay rod is less than 30 times of the diameter of the pull stay rod.
The thickness of the upper top plate and the lower bottom plate is calculated according to the formula35.3Mm was calculated.
And manufacturing an upper distributor and a lower distributor according to a schematic diagram 2, wherein the upper distributor and the lower distributor are made of S316L, the branch pipes are made of braided microporous pipes, and the upper distributor and the lower distributor are welded on the shell of the ion exchanger.
After the ion exchanger is manufactured and installed according to the conditions, anthracite particles with the specific gravity of more than or equal to 1.5g/cm 3 are paved on the lower bottom plate, and are paved on the lower distributor.
When in use, the macroporous anion exchange resin with the thickness of 0.35 mm-0.85 mm is filled, the filling amount is about 4.8m 3 on the horizontal tangent line of the upper distributor, 10.6m 3 percent sodium hydroxide (2.2 times of bed volume) is used for regenerating the resin, then the resin is washed until the effluent water is neutral, the resin is used for purifying 10 percent mannitol aqueous solution, the chromaticity after purification is less than or equal to 5PCU, and the chromaticity after the volume of the purified bed reaches 180BV is increased for regeneration treatment.
The chromaticity detection method comprises the following steps: on-line colorimeter
In this embodiment, 4.0% sodium hydroxide with 2.2 times of the bed volume is adopted as the regenerant to regenerate the resin, and the conventional exchanger generally adopts 4.0% sodium hydroxide with 3 times of the bed volume, but the regenerant actually contacting the resin is only 2.4 bed volumes, and after being used for purifying the mannitol aqueous solution, the chromaticity is the same as that of the conventional ion exchanger, the volume of the exchange bed can reach 180BV, and the conventional ion exchanger is the same, so that the regeneration and exchange effects of this embodiment are not lower than those of the conventional technology, and 27% of regenerant is saved.
The above embodiments can be seen that the following technical effects are achieved by the examples of the present invention:
after the flat plate type container structure is adopted, compared with a conventional ion exchanger with upper and lower sealing heads, the novel regenerant can be saved by about 20 percent, and meanwhile, the reverse regeneration of the waste regenerant on a resin layer is prevented, and the regenerant can be saved by 25 to 30 percent relatively.
After the special distributor and secondary distribution are adopted, the exchange and regeneration effects can be improved, and the purification quality can be improved.
The invention gets rid of the mechanical processing and mechanical limitation of the traditional elliptical head and the bearing plate, can be manufactured according to the process requirement, and avoids the phenomena of large occupied area, high investment and difficult operation caused by the parallel arrangement of large-sized Cheng Duotai ion exchangers.
While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the following claims be interpreted as including the preferred embodiments and all such alterations and modifications as fall within the scope of the invention.
It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof.
Claims (15)
1. An ion exchanger is characterized by comprising a shell (1), an upper top plate (2), a lower bottom plate (3), a pull stay bar (4), an upper distributor (6), a lower distributor (7) and a filling layer (5),
The upper top plate (2) and the lower bottom plate (3) are respectively arranged on the upper side and the lower side of the shell (1) along the radial direction, and a containing space is formed in the interior surrounded by the shell (1), the upper top plate (2) and the lower bottom plate (3);
The pull stay bar (4) is supported between the upper distributor (6) and the lower distributor (7);
the upper distributor (6) passes through one side of the shell (1) and is fixedly connected with part or all of the pull stay bars (4), and an inlet pipe of the upper distributor (6) is formed at one side of the upper distributor (6);
the lower distributor (7) passes through one side of the shell (1) and is fixedly connected with part or all of the pull stay bars (4), and an inlet pipe of the lower distributor (7) is formed at one side of the lower distributor (7);
the filling layer (5) is arranged above the lower bottom plate (3), the filling height of the filling layer (5) is higher than the upper horizontal tangent line of the lower distributor (7), and the filling layer (5) separates resin from the lower distributor (7) for secondary distribution.
2. The ion exchanger of claim 1, wherein the ion exchanger is used for anion exchange or cation exchange, and the material of the ion exchanger is selected according to two application conditions.
3. The ion exchanger of claim 1, wherein the housing is made of a metallic material selected from one of carbon steel, stainless steel, metallic titanium, cast iron alloy, having a diameter of 1.5m or more, a height of 1.5m or more, a wall thickness of +2mm or more, and a corrosion-resistant lining when exposed to corrosive media.
4. The ion exchanger according to claim 1, wherein the stay (4) is made of the same material as the casing (1), welded between the upper top plate (2) and the lower bottom plate (3), and is subjected to corrosion-resistant lining treatment when contacting a corrosive medium.
5. The ion exchanger according to claim 1 or 4, wherein the pull rods (4) are uniformly distributed in the accommodating space, the number is determined according to the diameter of the shell and the design pressure, the distance between the pull rods (4) and the shell (1) and the farthest distance between two adjacent pull rods (4) are smaller than 30 times the diameter of the pull rods (4), and the number is a positive integer greater than or equal to 1.
6. Ion exchanger according to claim 5, characterized in that the cross-sectional area of a single pull rod (4) is calculated according to the following formula:
a />
a, drawing the sectional area of a stay bar, and mm 2;
w is the axial load of a single pull stay rod, N;
[ sigma ] -allowable stress of pull-rod material at design temperature, MPa.
7. The ion exchanger according to claim 1, wherein the upper top plate (2) and the lower bottom plate (3) are of flat plate structure, are made of the same material as the shell (1), are welded with the shell (1), and are subjected to corrosion-resistant rubber lining treatment when contacting corrosive media.
8. The ion exchanger according to claim 1 or 4, wherein the upper top plate (2) and the lower bottom plate (3) are provided with holes in the same number and positions as the pull rods (4), and the pull rods penetrate through the holes and are welded with the upper top plate (2) and the lower bottom plate (3).
9. The ion exchanger according to claim 8, wherein the thicknesses of the upper top plate (2) and the lower bottom plate (3) are calculated according to the following formula:
Delta-thickness of the upper top plate (2) and the lower bottom plate (3), mm;
L is the distance between the pull stay bars (4) and the shell (1), and the farthest distance between two adjacent pull stay bars (4) is mm;
Pc-design pressure, MPa;
[ sigma ] -allowable stress of the material of the bottom plate (3) at the design temperature, MPa;
K is the connection method coefficient of the upper top plate (2) and the lower bottom plate (3).
10. The ion exchanger according to claim 1, wherein the lower distributor (7) is located above the lower bottom plate (3), and a tangential distance between an inlet pipe of the lower distributor (7) and the lower bottom plate (3) is 0-20 mm;
When the distributor is applied to a non-corrosive medium, the lower distributor (7) is the same as the shell (1), and an inlet pipe of the lower distributor (7) is welded on the shell (1); when the lower distributor (7) needs to be contacted with corrosive media, the lower distributor is made of acid-resistant materials, and is connected and sealed with the shell (1) by a stuffing box.
11. The ion exchanger according to claim 1, wherein the upper distributor (6) is located below the upper top plate (2), and the tangential spacing of the inlet pipe of the upper distributor (6) and the upper top plate (2) is calculated according to the following formula:
h, the tangential distance between the upper distributor (6) and the upper top plate (2) is mm;
HL, height of the shell (1), mm;
When the distributor is applied to a non-corrosive medium, the material of the upper distributor (6) is the same as that of the shell (1), and an inlet pipe of the upper distributor (6) is welded on the shell (1); when the upper distributor (6) needs to be contacted with corrosive media, the upper distributor is made of acid-resistant materials, and is connected and sealed with the shell (1) by a stuffing box.
12. The ion exchanger according to claim 10 or 11, wherein the lower distributor (7) and the upper distributor (6) adopt calandria distribution, the calandria comprises linear calandria or circular calandria, the calandria adopts one or more modes of micro-pore tube, macro-pore tube cladding gauze and wire winding tube, the tube gap of each calandria is selected to be between 0.15mm and 0.2mm, the discharge flow rate of the upper distributor (6) and the lower distributor (7) into the accommodating space is selected to be between 0.05m/s and 0.1m/s according to the maximum flow rate of exchange or regeneration, and the total flow rate of a distributor main pipe is selected to be between 1m/s and 1.5m/s.
13. The ion exchanger of claim 12, wherein the filling layer (5) is one or more of acid and alkali resistant anthracite particles, ceramic beads, glass beads and plastic beads, the specific gravity of the filling particles is more than or equal to 1.5g/cm 3, and the particle size is selected from micropore diameters, mesh openings of a cladding net and wire winding pipe gaps which are 5-10 times.
14. The ion exchanger of claim 1, wherein the ion exchanger is further provided with one or more conventional container assemblies selected from the group consisting of manholes, hand holes, safety valves, vent holes, and windows.
15. The ion exchanger according to claim 1, wherein the ion exchanger is adapted to fill the centre line of the upper distributor (6) with a chloride-type ion exchange resin during anion exchange and to fill the centre line of the upper distributor (6) with a sodium-type ion exchange resin during cation exchange.
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| CN203922760U (en) * | 2014-07-03 | 2014-11-05 | 江西省鑫盛钨业有限公司 | A kind of ion exchange unit of producing ammonium paratungstate |
| CN205035106U (en) * | 2015-08-25 | 2016-02-17 | 浙江华强环境科技有限公司 | High -efficient carbon ware that removes |
| CN207347223U (en) * | 2017-09-30 | 2018-05-11 | 常州海源恒业水处理设备有限公司 | The flat bottom cover cation and anion exchange device of a kind ofization water system equipment |
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2022
- 2022-05-24 CN CN202210568943.9A patent/CN115025824B/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB9102057D0 (en) * | 1991-01-31 | 1991-03-13 | Permutit Co Ltd | Ion exchange apparatus |
| EP0621239A2 (en) * | 1993-04-17 | 1994-10-26 | Judo Wasseraufbereitung GmbH | Small water treatment unit based on ion exchangers with possibility to regeneration and thermal desinfection |
| CN2530715Y (en) * | 2002-03-04 | 2003-01-15 | 南通市南宝石墨设备厂 | Filtering cap type chelating resin tower |
| CN202366713U (en) * | 2011-11-30 | 2012-08-08 | 河北瑞晶康生物科技有限公司 | Ion exchange column distributor |
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