CN103910411A - Solid bed, double bed and method for producing industrial demineralized water by taking solid bed and double bed as terminal demineralization equipment - Google Patents
Solid bed, double bed and method for producing industrial demineralized water by taking solid bed and double bed as terminal demineralization equipment Download PDFInfo
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- CN103910411A CN103910411A CN201410145893.9A CN201410145893A CN103910411A CN 103910411 A CN103910411 A CN 103910411A CN 201410145893 A CN201410145893 A CN 201410145893A CN 103910411 A CN103910411 A CN 103910411A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 155
- 238000005115 demineralization Methods 0.000 title claims abstract description 24
- 230000002328 demineralizing effect Effects 0.000 title claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 title claims description 13
- 239000007787 solid Substances 0.000 title abstract 5
- 239000011347 resin Substances 0.000 claims abstract description 165
- 229920005989 resin Polymers 0.000 claims abstract description 165
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 17
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 17
- 238000011049 filling Methods 0.000 claims abstract description 10
- 238000001223 reverse osmosis Methods 0.000 claims description 19
- 238000000108 ultra-filtration Methods 0.000 claims description 18
- 239000002245 particle Substances 0.000 claims description 13
- 238000007789 sealing Methods 0.000 claims description 9
- 229910001220 stainless steel Inorganic materials 0.000 claims description 9
- 239000010935 stainless steel Substances 0.000 claims description 9
- 238000007872 degassing Methods 0.000 claims description 7
- 239000013535 sea water Substances 0.000 claims description 5
- 238000012545 processing Methods 0.000 claims description 4
- 239000002131 composite material Substances 0.000 claims description 2
- 238000005342 ion exchange Methods 0.000 abstract description 23
- 238000000034 method Methods 0.000 abstract description 17
- 238000002360 preparation method Methods 0.000 abstract description 6
- 238000009826 distribution Methods 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000003957 anion exchange resin Substances 0.000 abstract 1
- 239000003729 cation exchange resin Substances 0.000 abstract 1
- 150000002500 ions Chemical class 0.000 description 27
- 230000008929 regeneration Effects 0.000 description 26
- 238000011069 regeneration method Methods 0.000 description 26
- 239000010410 layer Substances 0.000 description 20
- 238000010612 desalination reaction Methods 0.000 description 19
- 239000002585 base Substances 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 14
- 241000196324 Embryophyta Species 0.000 description 12
- 238000013461 design Methods 0.000 description 10
- 230000036632 reaction speed Effects 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 150000005837 radical ions Chemical group 0.000 description 8
- 239000002253 acid Substances 0.000 description 7
- 238000011068 loading method Methods 0.000 description 7
- 239000007790 solid phase Substances 0.000 description 6
- 238000005809 transesterification reaction Methods 0.000 description 6
- 239000003513 alkali Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 235000019600 saltiness Nutrition 0.000 description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 4
- 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 4
- 150000001450 anions Chemical class 0.000 description 4
- 150000001768 cations Chemical class 0.000 description 4
- 229910052802 copper Inorganic materials 0.000 description 4
- 239000010949 copper Substances 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 229910052710 silicon Inorganic materials 0.000 description 4
- 239000010703 silicon Substances 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 238000013459 approach Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000005012 migration Effects 0.000 description 3
- 238000013508 migration Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000002441 reversible effect Effects 0.000 description 3
- 241000209094 Oryza Species 0.000 description 2
- 235000007164 Oryza sativa Nutrition 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 150000001457 metallic cations Chemical group 0.000 description 2
- 230000005501 phase interface Effects 0.000 description 2
- 229920001296 polysiloxane Polymers 0.000 description 2
- 150000005838 radical anions Chemical class 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 235000009566 rice Nutrition 0.000 description 2
- -1 salt ion Chemical class 0.000 description 2
- 238000009736 wetting Methods 0.000 description 2
- 230000003245 working effect Effects 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
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- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000002939 deleterious effect Effects 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
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- 239000002356 single layer Substances 0.000 description 1
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Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention relates to an ion exchange resin demineralization device and method, and belongs to the technical field of preparation of industrial demineralized water. A solid bed comprises a resin bed body for being filled with ion exchange resin, and a water inlet and a water outlet formed in the resin bed body, wherein the resin bed body comprises an upper flange, a lower flange and a body wall surface; a cover plate and a bottom plate are arranged above and below the resin bed body; porous plates are arranged below the cover plate and/or above the bottom plate in the resin bed body respectively; a resin filling discharging port is formed in the body wall surface; a water distribution chamber is constructed by the space formed between the porous plates and the cover plate and/or the bottom plate; the water inlet and the water outlet are communicated with the water distribution chamber. The double bed comprises a cation exchange resin solid bed and an anion exchange resin solid bed formed by connecting in series. The double bed can be taken as ion exchange terminal demineralization equipment which meets the requirement of industrial demineralized water. The use of a mixed bed is eliminated in the preparation process of industrial demineralized water, and environmental protection is facilitated on every aspect.
Description
Technical field
The present invention relates to a kind of ion exchange resin desalination plant and method, belong to industrial de-mineralized water preparing technical field.
Background technology
Industry de-mineralized water is mainly used in thermal power generation boiler feedwater and chemical technique water, salt in the water of source is metallic cation and acid radical anion place solubilised state, can remove by spent ion exchange resin, in industrial de-mineralized water preparation field, custom calls cation bed (also claiming single of sun) the interchanger of filling Zeo-karb, the interchanger of filling anionite-exchange resin is called to anion bed (also claiming cloudy single), and a cation bed and this series combination of a pair of single of anion bed are called to multiple bed, again positive resin and two kinds of mixed with resin of negative resin are seated in to the mixed bed that calls of desalination in an interchanger.
When desalination, positive resin with commutative H ion and the negative resin with commutative OH radical ion exchange respectively (absorption) on positive resin or negative resin dissolved salts positive and negative ion in water, and the H ion and the OH radical ion that get off from resin exchange (desorb) can be combined into water molecules; Permutoid reaction is reversible, the metallic cation being attracted on positive resin can get off to discharge interchanger with the H ion-exchange in finite concentration acid solution, sun resin recovers the initial state preparation next cycle desalination of filled band H ion, in like manner, be attracted to acid radical anion on negative resin the OH radical ion in available finite concentration alkali lye exchange discharge interchanger, negative resin recovers the initial state preparation next cycle desalination of filled band OH root; The process of this recovery resin initial state is referred to as regeneration, and the chemical used of regenerating is called regenerator.
Ion exchange reaction is reversible reaction, and resin is in the time of desalination, and forward reaction speed is greater than backward reaction speed, and salt ion shows as and is adsorbed, and H ion or OH radical ion show as desorb; When regeneration, backward reaction speed is greater than forward reaction speed, and H ion or OH radical ion show as and be adsorbed, and salt ion shows as desorb.Whenever, positive reaction and reversed reaction are simultaneous, only have in the time that positive reaction speed is fully greater than reversed reaction speed, exchanger water just meets desalination index request.The multiple bed of single composition is in the time that desalination moves, H ion or OH radical ion that desorb is got off can participate in reversed reaction, when desalination proceeds to a certain degree, when in water, salt ionic concn is enough low, reversible ion exchange reaction reaches balance, desalination no longer carries out, so the desalination of multiple bed has certain limit; Mixed bed is by after two kinds of mixed with resin fillings of the negative resin of the positive resin of H type and OH, the H ion getting off from positive resin desorption when desalination and the OH radical ion getting off from negative resin desorb form water molecules in bed, in macroscopic view, see, if all H ion and OH radical ions are all combined into water molecules in mixed bed, backward reaction speed trend zero, positive and negative should be able to carrying through to the end, so desalination is thorough, effluent quality is good, and in theory, it is zero that mixed bed desalination can be used water concentration.
Easily, regenerator specific consumption is low in multiple bed regeneration, needs first the resin layering mixing when mixed bed regeneration, sun negative resin gets up to use with remix after acid-alkali regeneration respectively, operating process complexity, regenerator specific consumption is the more than 2.5 times of multiple bed, regeneration post-flush water the more than 5 times of multiple bed especially; But mixed-bed effluent quality is good, according to the multiple bed feature different from mixed bed, the way of custom is as elementary demineralization plant by multiple bed, the aliquant few part salt of multiple bed just allows mixed bed go to bear, so mixed bed is often as the last terminal demineralization plant that ensures water quality, comparatively ripe current of reverse osmosis technology, existing reverse osmosis is replaced to the trend of multiple bed as elementary demineralization plant, terminal demineralization plant is often or mixed bed.
Ion-exchange unit is generally vertical type cylinder type container, resin is deposited in container with state of nature, certain space is left on container top, do expand cleaning of resin, when equipment operation or regeneration, resin layer transfixion, need the water of desalination to flow to from one end of cylinder shape equipment, the other end flows out, when operation, ion exchange resin successively lost efficacy in water (flow) direction, iff for water outlet up to standard, according to different operating modes, ion exchange resin raising just can be accomplished to 60 centimetres at 30 centimetres, but because ion exchange resin need to periodically be regenerated with regenerator, and traditional regeneration is all generally manual operation, need certain skill level and there is certain labour intensity, so, often adopt the method for many loaded resins in interchanger to obtain the longer cycle of operation (design specifications requires to reach 24 hour cycle of operation at present), moreover, because being nature, stacks resin layer, if resin layer is too thin, under the effect of pressure water, in resin layer, easy formation directly penetrates the water stream channel (being commonly called as channel) of resin layer, impact exchange effect and effluent quality greatly, generally, resin layer raising is designed to 2 meters or higher, in addition, resin layer also needs to carry out backwash with clear water, single of internal regeneration can arrange the backwash expansion space that accounts for resin loadings 50-70%, for there being good layered effect, internal regeneration mixed bed arranges and accounts for the more than 100% backwash expansion space of resin loadings, so, no matter be single or mixed bed, interchanger container virtual height generally needs 3-4 rice or higher, equipment total height reaches 6-8 rice or higher.
CN103496806A (2014-1-8) discloses a kind of de-mineralized water production system and de-mineralized water production method, but it is also to adopt the multiple bed of tradition to process as the intermediate stage, can not serve as terminal demineralization plant and use, its terminal demineralization plant is also mixed bed.
If producing in de-mineralized water technique, ion exchange method can not establish mixed bed, and only with just effluent quality index request definitely of multiple bed, that will make ion-exchange demineralization technique not only become simpler and more direct, ion exchange resin regeneration soda acid consumption used also will reduce greatly, and the application advantage of ion exchange technique in industrial de-mineralized water is produced will be more obvious.
Summary of the invention
One of object of the present invention is to provide a kind of real bed as ion-exchange demineralization equipment.
Two of object of the present invention is to provide a kind of multiple bed that can serve as industrial de-mineralized water terminal demineralization plant.
Three of object of the present invention is to provide a kind of industrial de-mineralized water production method using multiple bed as terminal demineralization plant.
The first technical purpose of the present invention is achieved by the following technical programs:
A kind of real bed, comprise for the resin bed body of filling ion-exchange resin and be arranged on water-in and the water outlet on described resin bed body, described in it, resin bed body is for comprising upper flange, the resin bed body of lower flange and body wall, the described resin bed body cover plate of the described upper flange of sealing and the base plate of the described lower flange of sealing of being useful on setting up and down, in described resin bed body and be positioned at cover plate below and/or base plate top and be respectively arranged with for making into water or water outlet is uniformly distributed and unlikely resin is escaped microwell plate, on described body wall, be provided with resin fill (discharging) mouth and plug, the space forming between described microwell plate and cover plate and/or base plate forms distributing water room, described water-in and water outlet are connected with described distributing water room.
Arrange by structure of the present invention:
Resin layer is not that nature is stacked in bed, but fully tamp with pump, when filling, resin mixes by a certain percentage with de-salted water, inject from a real bed resin fill mouth being mixed in resin in de-salted water with water pump, water is drained resin from water-in and water outlet and is stayed in bed, when filling, as required, pump outlet pressure is that stowing pressure P is between 0.15-0.5MPa, and operating pressure need to be between the 1.5-3.0 of resin fill pressure times, after resin tamps, close contact between resin particle, extruding mutually, when operation, current are extruded between resin particle under larger pressure, exchangable ion infinite approach in current intermediate ion and resin particle, ion migration distance diminishes, ion exchange reaction speed is improved, effluent quality is better.Because resin layer tamps, so this resin bed is called to real bed;
The resin layer feedwater flow being tamped has formed certain resistance, make distributing water room be all the time full water state, the water getting off from distributing water room flows to resin layer equably by microwell plate, because resin layer tamps, even the in the situation that, resin layer high at flow velocity being thin, also can not form channel, allow often ooze water and have the chance through abundant ion-exchange, effluent quality is more guaranteed;
Traditional ion-exchanger long-term operation, based in manual regenerative operation situation, from reducing labour intensity, be convenient to production management aspect consider design, since over half a century, this using method adopts so far and is accustomed to always, has become the mindset of China's ion-exchange unit design, and popular design specifications requires the equipment cycle of operation to be not less than 24 hours.In automated operation degree very high present age, this design concept there is no need to adhere to completely again.The real bed of the present invention adopts the less than short period of 1 hour operation design, makes resin loadings less than original 1/10th.Owing to being real bed, fluid is large by the comparison of resistance of resin layer, adopts after short-period design concept, and resin is loaded as far as possible less, and lathe bed is as far as possible short, thereby makes current be unlikely to too large by the resistance of real bed, just can have better actual motion effect.Lathe bed is short, has not only greatly reduced resin demand, and makes high flow rate become possibility, the further attenuate of high flow rate resin particle surface detention layer thickness, make the total velocity of ion exchange of resin layer higher, exchange better effects if.Void column flow velocity of the present invention reaches 30-80 m/h, and not only attenuate resin particle surface detention layer thickness also makes equipment aquifer yield larger (single design current velocity 15-25 m/h of tradition) accordingly.
Resin is in desalting process, exchangable ion on resin not all participates in permutoid reaction, on resin, the total quantity of exchangable ion characterizes with complete exchange capacity, the quantity of the exchangable ion of actual participation desalination is operating capacity, in certain resin, the rate of exchange of each exchangable ion is different, the exchangable ion rate of exchange that approaches resin solid phase interface is large, the exchangable ion rate of exchange of going deep into solid phase inside is little, in rate of exchange and resin solid phase, the quadratic power of migration distance is inversely proportional to, approach the exchangable ion that resin solid phase interface rate of exchange is large and first participate in permutoid reaction, and develop to solid phase depths by rear permutoid reaction district, what the planner of conventional resins bed pursued is larger operating capacity and longer work period, allow the exchangable ion of resin solid phase as much as possible depths also participate in permutoid reaction, this certainly will make the total rate of exchange of resin bed reduce, exchange deleterious, effluent quality is deteriorated, in actual motion, according to different operating modes, tradition monobed resin operating capacity approximately reaches the 50-55% of complete exchange capacity, and the present invention is set in traditional below 1/4th (be approximately less than resin complete exchange capacity 12%) resin operating capacity, few in aforementioned resin filling, short period operation situation under, the cycle of operation is set shortlyer, according to different operating modes, the cycle of operation is between 20-40 minute, make single better effects if.
Resin operating capacity is set little, also mean that degree of percent regeneration of resin is low, during with operation, transesterification reaction rate is high the same, when regeneration, speed of reaction is high too, thereby as long as use the regenerator that is slightly larger than operating capacity just can complete regeneration, the effect of bringing is that regenerator specific consumption is low, regenerator specific consumption is below 1.1 (1.1 to 1, operating capacity is 1, regenerator actual amount is 1.1), conventionally the regenerator specific consumption of single is between 1.4-1.6, and mixed bed is greater than 4.0, has greatly saved regenerator; Because be real bed, counter-current regeneration flow velocity can be enough large, and large to approaching operation flow velocity, so the regeneration used time is short, general, the recovery time of one single is less than 4 minutes.
The reality bed of the inventive method manufacture makes an interior ion exchange reaction fully, rapidly, efficiently, and for producing industrial de-mineralized water, effluent quality is good guaranteed again, also saves regenerator.
As preferably, the distance between upper and lower two microwell plates of described resin bed is that resin loading height is 10-20 centimetre.
As preferably, the resin particle diameter in described resin bed body is the gel type resin of 0.1-0.3 millimeter.
In the present invention, resin loading height is little, under high flow rate, move again, so current are by the time very short (as 5 seconds) of resin layer, necessarily require transesterification reaction rate high, concerning gel type resin, because the transesterification reaction rate of certain ion and this ion square being inversely proportional to of ion migration distance in resin particle in resin, the specific surface area of ball-type resin is inverse ratio with resin particle diameter again, so, when resin particle diameter hour, the near surperficial exchangable ion accounting that on resin, transesterification reaction rate is large is just larger, set hour at aforementioned operating capacity, still have the near surperficial exchangable ion that abundant transesterification reaction rate is large to participate in permutoid reaction, entirety has improved the transesterification reaction rate of resin bed, ensure better water outlet quality.
Real bed requires resin particle to be depressed into deformation to a certain degree, and resin must have good physical strength, and the present invention should adopt the gel-type spheroidal resin that coefficient of uniformity is higher.
As preferably, in the distributing water room forming between described microwell plate and described cover plate or base plate, be provided with strut member, be delivered to cover plate or base plate for pressure that resin layer is acted on microwell plate, strut member can be fixed on supporting post-rod on described cover plate or base plate or with cover plate or the unfixed independent support part of base plate.
Arranging of supporting post-rod or independent support part can prevent microwell plate distortion.
As preferably, the stainless steel cylinder that described resin bed body is upper and lower opening, described microwell plate is that thickness is the MULTILAYER COMPOSITE flat board with the micropore sintered plate of stainless steel of 1-8mm.
Select the micropore sintered plate of stainless steel cylinder and stainless steel multilayer, can be corrosion-resistant, to gain in strength, opposing water impact, increases work-ing life.Certainly,, if the thickness of the micropore sintered plate of stainless steel can reach requirement of strength, single layer structure also can be realized.
As preferably, described cover plate and/or base plate and described resin bed body are fixed by mounting block and seal by sealing member, and described mounting block comprises bolt, nut and pad, and described sealing member comprises seal washer.
More preferably, described microwell plate and described resin bed cylindrical shell are welded with the leakage barriers that prevents that resin from revealing around.
The second technical purpose of the present invention is achieved by the following technical programs:
A multiple bed, it comprises the real bed of Zeo-karb and the real bed of anionite-exchange resin that series connection forms.
The multiple bed that the present invention is made up of real bed significantly improves the effluent quality of the multiple bed of ion exchange resin, and when operation, upper entering and lower leaving, adopts counter-current regeneration when regeneration, and the regeneration of anionite-exchange resin adopts the heat alkali liquid of 50-60 DEG C, enters upper row under regenerator.
As preferably, the real bed of Zeo-karb that the multiple bed of the present invention is series connection adds degassing tower and adds the real bed of anionite-exchange resin, and in the time that multiple bed water inlet bicarbonate ion concentration is greater than 100mg/l, recommendation is selected especially.
Because the water outlet of the multiple bed of the present invention can directly reach the index request of industrial de-mineralized water to each relevant ions content, in de-mineralized water preparation technology, can not establish mixed bed, and only with multiple bed just definitely effluent quality index request, this will make ion-exchange demineralization technique become simple and direct, equipment cost is lower, resin demand still less, simultaneously, the present invention also reduces ion exchange resin regeneration soda acid consumption greatly, regeneration waste liquid generation is less, adopts the present invention to make the application advantage of ion exchange technique in industrial de-mineralized water is produced larger.
The 3rd technical purpose of the present invention is achieved by the following technical programs:
A kind of multiple bed is as the industrial de-mineralized water production method of terminal desalination, it is that former water is obtained to ultrafiltration water outlet after ultrafiltration apparatus is processed, then described ultrafiltration water outlet is sent into after the real bed of Zeo-karb is processed and obtained the first water outlet, more described the first water outlet is sent into and after the real bed of anionite-exchange resin is processed, obtained the second water outlet and be required industrial de-mineralized water; The empty bed flow velocity of the real bed of described anionite-exchange resin or the real bed of Zeo-karb is 30-80 m/h.
The present invention is packed into real bed with the higher small-particle resin of coefficient of uniformity by the cation bed of the multiple bed of composition and anion bed, adopt the operation means such as short period design is high with operation flow velocity, timely regeneration, the total ion exchange reaction speed of resin bed is improved greatly, water intermediate ion is removed more thoroughly, water outlet quality is better, thereby reach the object that allows the multiple bed of full mold become industrial de-mineralized water terminal demineralization plant, in industrial de-mineralized water reparation technology, can thoroughly remove from office mixed bed.
The inventive method is under routine water inlet saltiness condition, according to adopting reverse osmosis or not adopting the different operating modes of the pre-desalination of reverse osmosis, multiple bed water outlet resistivity can reach and be greater than 5-10 megaohm centimetre above (being that electrical conductivity of water is less than 0.2-0.1 μ s/cm), going out the water hardness is 0, according to the difference of former water silicone content, water outlet silicone content is less than 5-20 μ g/l, can meet the requirement of subcritical superhigh pressure boiler supplementary feed to former water desalination completely.In addition, the present invention not only replaces a mixed bed to reduce regenerator specific consumption with the multiple bed of full mold, and resin demand is few compared with the multiple bed of tradition of the multiple bed of full mold of the present invention and same diameter, aquifer yield is larger, regenerator specific consumption is lower.
As preferably, between the real bed of Zeo-karb and the real bed of anionite-exchange resin, add degassing tower, after processing, ultrafiltration apparatus sends into the real bed of Zeo-karb by former water, degassing tower is sent in the water outlet of the real bed of Zeo-karb, the real bed of anionite-exchange resin is sent in degassing tower water outlet, and the water outlet of the real bed of anionite-exchange resin is industrial de-mineralized water.
As preferably, former water after processing, ultrafiltration apparatus is obtained to ultrafiltration water outlet, then described ultrafiltration water outlet is sent into reverse osmosis equipment and processed and obtain reverse osmosis water outlet, and then obtain industrial de-mineralized water after described reverse osmosis water outlet is processed by the real bed of described Zeo-karb and the real bed of anionite-exchange resin successively.
More preferably, described former water is seawater, and described reverse osmosis equipment comprises first-stage reverse osmosis and the second level reverse osmosis apparatus of series connection.
The ion-exchange demineralization wetting system that the inventive method is manufactured, lathe bed is short, and equipment is small and exquisite, and materials economize, lightweight, can laminated multi-layer, after employing, will greatly reduce factory building area occupied and equipment, factory building total investment expenses; Simultaneously also reduced the consumption of resin, if applied, also will greatly reduce with serious pollution ion exchange resin factory industrial scale, economic benefit and social enviroment protection effect are remarkable.
In sum, the present invention has following beneficial effect:
The present invention removes from office and has gone mixed bed in industrial de-mineralized water reparation technology, to answer bed as ion-exchange terminal demineralization plant, make ion-exchange demineralization equipment become simpler and easy, automatic control program is simpler, the regenerator specific consumption of resin regeneration is lower, compared with mixed bed, has greatly reduced the consumption of regenerated acid and alkali, also the discharge capacity that has reduced acidic and alkaline waste water, is conducive to environmental protection.
The ion-exchange demineralization wetting system that the present invention manufactures, lathe bed is short, and equipment is small and exquisite, has greatly saved device fabrication materials, will greatly reduce factory building and take up an area and build and invest after employing.
After the present invention is applied; to greatly reduce the consumption of ion exchange resin, it is heavy polluted industry that ion exchange resin is produced, and the present invention is in reducing ion exchange resin consumption; also by the industrial scale of reduction ion-exchange factory, be conducive to generally environment protection.
Brief description of the drawings
Fig. 1 be the real bed of the present invention partly cut open front view;
Fig. 2 is the schematic diagram of the multiple bed of the present invention;
Fig. 3 is that the industrial de-mineralized water of an embodiment of the present invention is produced system;
Fig. 4 is that the industrial de-mineralized water of the another kind of embodiment of the present invention is produced system;
Fig. 5 is that the industrial de-mineralized water of the third embodiment of the present invention is produced system.
Fig. 6 is that the industrial de-mineralized water of the 4th kind of embodiment of the present invention is produced system.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
As shown in Figure 1, real bed comprises for the resin bed body 1 of filling ion-exchange resin and is arranged on water-in 2 and the water outlet 3 on resin bed body 1, resin bed body 1 comprises upper flange 11, the resin anion(R.A) bed body of lower flange 12 and body wall 13 or resin cation (R.C.) bed body, resin bed body 1 is respectively arranged with up and down the cover plate 4 for sealing upper flange 11 and seals the base plate 5 of lower flange 12, cover plate 4 and/or base plate 5 are fixed and are sealed by sealing member by mounting block 9 with resin bed body 1, mounting block comprises bolt, nut and pad, sealing member comprises seal washer.Real bed adopts short period such as operation design in 30 minutes, so resin loadings is few, loading height only has 10-20 centimetre.Resin particle diameter in resin bed body is 0.1-0.3 millimeter.
In resin bed body 1 and be positioned at cover plate 4 belows and/or base plate 5 tops and be respectively arranged with for making and, into water or the equally distributed microwell plate 6 of water outlet, be provided with resin fill mouth 7 on body wall 13.Resin fill mouth 7 can be the inlet that carries sealing member, also can on resin fill mouth 7, install in addition plug additional, and resin clip water is blocked filling mouth after pumping into and tamping.
The space forming between microwell plate 6 and cover plate 4 and/or base plate 5 forms distributing water room 8, and water-in 1 and water outlet 2 are connected with distributing water room 8.
Resin bed body can be rectangular parallelepiped or cylinder, is preferred for the stainless steel cylinder of upper and lower opening; Because flow velocity in bed body is fast, pressure is large, and for water distribution effectively, microwell plate can not be too thick, too thinly can reduce real bed work-ing life, considers the micropore sintered plate of stainless steel that it is 1.5-2mm that microwell plate is selected as thickness.In order more effectively to support thinner micropore sintered plate, between microwell plate 6 and cover plate 4 or base plate 5, be provided with the strut member 10 for supporting microwell plate 6.Strut member 10 can be the multiple supporting post-rods that are fixed on cover plate 4 or base plate 5, can be also unfixed single independent support part.
As shown in Figure 2, multiple bed is made up of real bed, comprises the real bed 16 of Zeo-karb and the real bed 17 of anionite-exchange resin that series connection forms.When operation, upper entering and lower leaving; When regeneration, adopt counter-current regeneration, under regenerator, enter upper row.Adopt acid solution to regenerate to the real bed 16 of Zeo-karb, adopt the heat alkali liquid of 50-60 DEG C to regenerate to the real bed 17 of anionite-exchange resin, the liquid after manipulation of regeneration flows into neutralization tank processing.Without mixed bed, the multiple bed of the one-level water outlet of real bed composition just reaches the de-mineralized water index that superhigh pressure boiler supplementary feed requires.
Embodiment mono-
As shown in Figure 3, be less than by saltiness the source water that 200mg/l, heavy carbonic root be less than 50mg/l and produce industrial de-mineralized water.Former water is successively after ultra-filtration equipment 14, the real bed 16 of Zeo-karb and the real bed 17 of anionite-exchange resin, and water outlet reaches industrial de-mineralized water index request, and effluent quality is: specific conductivity=0.2 μ S/cm, hardness=0, iron=0, copper=0, sodium=5 μ g/l, silicon=15 μ g/l.
Embodiment bis-
As shown in Figure 4, be less than by saltiness the source water that 300mg/l, heavy carbonic root be greater than 100mg/l and produce industrial de-mineralized water.Source water is successively after ultra-filtration equipment 14, the real bed 16 of Zeo-karb, decarbonation tower 18, pump 19, the real bed 17 of anionite-exchange resin, water outlet reaches industrial de-mineralized water index request, effluent quality is: specific conductivity=0.2 μ S/cm, hardness=0, iron=0, copper=0, sodium=5 μ g/l, silicon=15 μ g/l.
Embodiment tri-
As shown in Figure 4, produce industrial de-mineralized water by saltiness at the source of 200-5000mg/l water.Source water is successively after ultra-filtration equipment 14, reverse osmosis unit 15, the real bed 16 of Zeo-karb and the real bed 17 of anionite-exchange resin, and water outlet reaches industrial de-mineralized water index request, and effluent quality is: specific conductivity=0.1 μ S/cm, hardness=0, iron=0, copper=0, sodium=3 μ g/l, silicon=5 μ g/l.
Embodiment tetra-
As shown in Figure 5, produce industrial de-mineralized water, seawater saltiness 35000mg/l with seawater.Seawater is successively after ultra-filtration equipment 14, first-stage reverse osmosis device 151, second level reverse osmosis apparatus 152, the real bed 16 of Zeo-karb and the real bed 17 of anionite-exchange resin, and water outlet reaches industrial de-mineralized water index request.Effluent quality is: specific conductivity=0.1 μ S/cm, hardness=0, iron=0, copper=0, sodium=5 μ g/l, silicon=3 μ g/l.
This specific embodiment is only explanation of the invention; it is not limitation of the present invention; those skilled in the art are reading after this specification sheets and can make to the present embodiment the amendment that there is no creative contribution as required, but as long as within the scope of claim of the present invention, are all subject to the protection of patent law.
Claims (10)
1. real bed, comprise for the resin bed body (1) of filling ion-exchange resin and be arranged on water-in (2) and the water outlet (3) on described resin bed body (1), it is characterized in that: described resin bed body (1) is for comprising upper flange (11), lower flange (12) and body wall (13), described resin bed body (1) is respectively arranged with up and down the cover plate (4) for sealing described upper flange (11) and seals the base plate (5) of described lower flange (12), in described resin bed body (1) and be positioned at cover plate (4) below and/or base plate (5) top and be respectively arranged with for making into water or water outlet is uniformly distributed and unlikely resin is escaped microwell plate (6), on described body wall (13), be provided with resin fill discharge opening (7), the space forming between described microwell plate (6) and described cover plate (4) and/or base plate (5) forms distributing water room (8), described water-in (2) and water outlet (3) are connected with described distributing water room (8).
2. a kind of real bed according to claim 1, is characterized in that: the distance between upper and lower two microwell plates of described resin bed is 10-20 centimetre.
3. a kind of real bed according to claim 2, is characterized in that: the resin particle diameter in described resin bed body is 0.1-0.3 millimeter.
4. a kind of real bed according to claim 3, is characterized in that: between described microwell plate (6) and described cover plate (4) or base plate (5), be provided with the strut member (10) for supporting described microwell plate (6).
5. a kind of real bed according to claim 4, is characterized in that: the stainless steel cylinder that described resin bed body is upper and lower opening, described microwell plate is that thickness is the MULTILAYER COMPOSITE flat board with the micropore sintered plate of stainless steel of 1-8mm.
6. the multiple bed forming according to the real bed of claim 1-5 any one, is characterized in that: it comprises real of Zeo-karb and the real bed of anionite-exchange resin that series connection forms.
7. a multiple industrial de-mineralized water production method as terminal demineralization plant according to claim 6, it is characterized in that: former water is obtained to ultrafiltration water outlet after ultrafiltration apparatus is processed, then described ultrafiltration water outlet is sent into after the real bed of Zeo-karb is processed and obtained the first water outlet, more described the first water outlet is sent into and after the real bed of anionite-exchange resin is processed, obtained the second water outlet and be required industrial de-mineralized water; The empty bed flow velocity of the real bed of described anionite-exchange resin or the real bed of Zeo-karb is 30-80 m/h.
8. a multiple industrial de-mineralized water production method as terminal demineralization plant according to claim 6, it is characterized in that, between the real bed of Zeo-karb and the real bed of anionite-exchange resin, add degassing tower, after processing, ultrafiltration apparatus sends into the real bed of Zeo-karb by former water, degassing tower is sent in the water outlet of the real bed of Zeo-karb, the real bed of anionite-exchange resin is sent in degassing tower water outlet, and the water outlet of the real bed of anionite-exchange resin is industrial de-mineralized water.
9. a multiple industrial de-mineralized water production method as terminal demineralization plant according to claim 7, it is characterized in that: former water is obtained to ultrafiltration water outlet after ultrafiltration apparatus is processed, then described ultrafiltration water outlet is sent into reverse osmosis equipment and processed and obtain reverse osmosis water outlet, and then obtain industrial de-mineralized water after described reverse osmosis water outlet is processed by the real bed of described Zeo-karb and the real bed of anionite-exchange resin successively.
10. multiple bed according to claim 9, as an industrial de-mineralized water production method for terminal demineralization plant, is characterized in that: described former water is seawater, and described reverse osmosis equipment comprises first step reverse osmosis unit and the second stage reverse osmosis unit of series connection.
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| CN201410145893.9A CN103910411B (en) | 2014-04-14 | 2014-04-14 | Real bed, multiple bed and the industrial de-mineralized water production method as terminal demineralization plant thereof |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019041741A1 (en) * | 2017-08-30 | 2019-03-07 | 浙江兴禹环境科技有限公司 | Solid bed with movable pressing plate |
| CN114314753A (en) * | 2021-12-27 | 2022-04-12 | 湖南金牛化工有限公司 | Alkali-saving type anion bed regeneration treatment method |
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| CN102001727A (en) * | 2010-12-24 | 2011-04-06 | 华电水处理技术工程有限公司 | Ion exchange equipment |
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| CN86101606A (en) * | 1985-05-06 | 1986-11-05 | 埃科-泰克有限公司 | Fluid treatment method and equipment |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2019041741A1 (en) * | 2017-08-30 | 2019-03-07 | 浙江兴禹环境科技有限公司 | Solid bed with movable pressing plate |
| CN114314753A (en) * | 2021-12-27 | 2022-04-12 | 湖南金牛化工有限公司 | Alkali-saving type anion bed regeneration treatment method |
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| CN103910411B (en) | 2015-11-04 |
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