CN101774716B - Water treatment method and device using aluminum oxide secondary condensation water as make-up water of power plant - Google Patents
Water treatment method and device using aluminum oxide secondary condensation water as make-up water of power plant Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 215
- 238000000034 method Methods 0.000 title claims abstract description 33
- 238000009833 condensation Methods 0.000 title claims abstract description 26
- 230000005494 condensation Effects 0.000 title claims abstract description 26
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 title claims abstract description 19
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 40
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 38
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 34
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000004411 aluminium Substances 0.000 claims abstract description 32
- 150000002500 ions Chemical class 0.000 claims abstract description 27
- 150000001450 anions Chemical class 0.000 claims abstract description 22
- 150000001768 cations Chemical class 0.000 claims abstract description 22
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 19
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 19
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003245 coal Substances 0.000 claims abstract description 11
- 238000005342 ion exchange Methods 0.000 claims abstract description 11
- 238000001914 filtration Methods 0.000 claims abstract description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 52
- 238000007667 floating Methods 0.000 claims description 47
- 238000005273 aeration Methods 0.000 claims description 46
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims description 33
- 230000008929 regeneration Effects 0.000 claims description 19
- 238000011069 regeneration method Methods 0.000 claims description 19
- 238000005189 flocculation Methods 0.000 claims description 18
- 230000016615 flocculation Effects 0.000 claims description 18
- 239000000701 coagulant Substances 0.000 claims description 15
- 239000000835 fiber Substances 0.000 claims description 13
- 239000004576 sand Substances 0.000 claims description 13
- 239000000377 silicon dioxide Substances 0.000 claims description 13
- 239000002253 acid Substances 0.000 claims description 12
- 239000003795 chemical substances by application Substances 0.000 claims description 12
- 238000012545 processing Methods 0.000 claims description 12
- 239000003513 alkali Substances 0.000 claims description 11
- 235000006408 oxalic acid Nutrition 0.000 claims description 11
- 210000000476 body water Anatomy 0.000 claims description 10
- 239000000706 filtrate Substances 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 7
- 239000002893 slag Substances 0.000 claims description 7
- 230000015556 catabolic process Effects 0.000 claims description 6
- 239000000356 contaminant Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 238000006731 degradation reaction Methods 0.000 claims description 6
- 238000010612 desalination reaction Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 230000001172 regenerating effect Effects 0.000 claims description 4
- 125000002091 cationic group Chemical group 0.000 claims description 3
- 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 abstract description 7
- 239000003456 ion exchange resin Substances 0.000 abstract description 7
- 229920003303 ion-exchange polymer Polymers 0.000 abstract description 7
- 239000006004 Quartz sand Substances 0.000 abstract 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 abstract 1
- 239000003830 anthracite Substances 0.000 abstract 1
- 230000000593 degrading effect Effects 0.000 abstract 1
- 239000003344 environmental pollutant Substances 0.000 abstract 1
- 230000003311 flocculating effect Effects 0.000 abstract 1
- 239000000463 material Substances 0.000 abstract 1
- 231100000719 pollutant Toxicity 0.000 abstract 1
- 235000010210 aluminium Nutrition 0.000 description 26
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 9
- 229910052742 iron Inorganic materials 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000011160 research Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 230000003020 moisturizing effect Effects 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 230000003245 working effect Effects 0.000 description 2
- 239000004912 1,5-cyclooctadiene Substances 0.000 description 1
- REDXJYDRNCIFBQ-UHFFFAOYSA-N aluminium(3+) Chemical compound [Al+3] REDXJYDRNCIFBQ-UHFFFAOYSA-N 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
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- 238000005188 flotation Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
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- 231100000252 nontoxic Toxicity 0.000 description 1
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- 239000000047 product Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
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- 239000008400 supply water Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses a water treatment method and device using aluminum oxide secondary condensation water as make-up water of power plant. The water treatment method comprises the following steps: reducing the temperature of secondary condensation water from an aluminium oxide factory, degrading pollutants, flocculating, performing floatation, filtering and performing ion exchange, wherein after a floatation device is used for primary aluminum removal, a two-medium mechanical filter is used to remove residual aluminum; the mechanical filter adopts anthracite coal and quartz sand as filter materials and is used to remove most of aluminium in water passing through the floatation device so that the content of aluminium in water meets the standard that the content of aluminium is less than 0.3 mg/L and the problem that when the content of aluminium is too high, the subsequent ion exchange resin is polluted, is avoided. The filtered water of which aluminium content is less than 0.3 mg/L enters a cation exchanger, a carbon dioxide remover, an anion exchanger and a mixed ion exchanger in turn, the effluent can be used as the make-up water of a high-pressure boiler, and water processed by the device completely meets the make-up water standard of the high-pressure boiler.
Description
Technical field
The invention belongs to water treatment field, relate to a kind of water of condensation treatment process and device, especially a kind of aluminum oxide secondary condensed water is as the water treatment method and the device of power-plant makeup.
Background technology
The eighties in last century, time condensation water only is confined to be back to life and produces the miscellaneous water level, and reuse technology research is less.After the nineties in last century, time condensation water progressively is used for high quality high-quality miscellaneous water, and reuse technology research is more, and application obtains many progress.So far, domestic existing with the instance that is used for the middle low-pressure boiler feedwater after the time condensation water treatment.But recognize through investigation; This project is not done complete water quality analysis to time condensation water; Water quality is also inadequate to the influence research of IX advanced treatment, and this treatment project exists exchange resin weak point in work-ing life, resin to change a series of problems such as frequency height, working cost height after directly adopting IX without the pre-treatment of necessity; Therefore, can think that existing practical applications is to be based upon to sacrifice on the basis that ion exchange resin is cost to implement.Up to now, do not see as yet the instance of time condensation water handling reclamation to the high-duty boiler moisturizing.
At present, the aluminum oxide secondary water of condensation is handled and to be back to boiler feedwater and to be applied in domestic still immaturely, drops into and uses lessly, especially handles and is used for the high-duty boiler supplementary feed blank is beyond example at home.Therefore; The research topic challenge of time condensation water handling reclamation this thinking of pioneering and inventing in boiler feedwater is big; Strive breakthrough and innovation, dare to being the people that domestic first hand " is eaten crab ", it is blank not only will to fill up domestic industry; Also will establish the model of " energy-saving and emission-reduction " to the enterprise and the same industry, meaning is very great.
From water-quality ratio, time condensation water is the fine de-salted water, and it is handled as the high-duty boiler supplementary feed, and the technical prime demineralising process that saves also is very worthwhile economically.But time condensation water technology difficult point is following:
(1) selection of effective removal method of heavy metal ion.Particularly possibly bring the removal of the shape aluminiums such as trivalent aluminium ion in the water in the aluminum oxide production process into, though iron level is lower in the water quality report, iron pipeline etc. can influence iron level inevitably in the production run, so also must consider the removal of iron level.
(2) CODMn content is still higher in the water-quality guideline, and certain Organic pollutants are still arranged, and does not thoroughly remove also will produce subsequent technique to have a strong impact on.
(3) though contain oil index in the water and do not detect; But should admit; This water quality report is merely an appearance result, because must there be mechanical means such as water pump, blower fan, stirrer to contact with time condensation water in the production run, also has the oil pollution that possibly bring in the overhaul of the equipments process simultaneously.In addition; Bauxite ore is along with influences such as the mineral products place of production, geologic conditions, and the mineral resources that will have the resinous shale class gets in the production process, and aluminum oxide is in the stripping evaporative process; May produce the oil pollution of resinous shale class; To constitute a latent danger to water quality, therefore, anti-oil pollution is one of important content in the pre-treatment control.
(4) in the pretreatment technology process, the pH in must strict control water is in the scope of 6-8, otherwise aluminium, iron, oil, COD
MnEtc. water-quality guideline difficulty is controlled within the requirement.
(5) quality of pretreatment technology treatment effect directly exerts an influence to capacity, life-span and the regeneration level of ion exchange resin.The IX water inlet condition of controlling well is the guarantee of ion exchange resin good operation.Though analysis and assessment are thought, even Al
3+In 1～2mg/L scope, ion exchange resin also can keep in the timeliness in 3～5 years work-ing life, but technological test requires still will aluminium, iron, wet goods water-quality guideline be controlled within the 0.3mg/L.
Summary of the invention
The objective of the invention is to overcome the shortcoming of prior art; Remedy in the prior art blank that time condensation water further is applied to the high-duty boiler moisturizing; Overcome the difficult point of alumina evaporation time condensation water treatment, water treatment method and the device of a kind of aluminum oxide secondary condensed water as power-plant makeup are provided.Art breading and the rational flocculation agent prescription of this method through optimizing; Make time condensation water reach the requirement of high-duty boiler moisturizing; Cooperate this method design one cover water treatment device; This device adopts common equipment to carry out the reasonable optimizing winding, has effectively realized water treatment method of the present invention, and has effectively improved the efficient of water treatment.
The objective of the invention is to solve through following technical scheme:
This aluminum oxide secondary condensed water is characterized in that as the water treatment method of power-plant makeup, may further comprise the steps:
1) cooling, degradation of contaminant:
The time condensation water that alumina producer is come feeds the aeration tank and carries out aeration after surface-type heat exchanger heat exchange to 35 ℃, and the GWR of aeration is 7: 1;
2) flocculation, air supporting:
Water behind the aeration gets into air-floating apparatus through pipeline self and carries out the air supporting processing; On the inlet tube of air-floating apparatus, at first add hydrochloric acid and regulate pH value to 6～8 of water, add PAC flocculation agent or oxalic acid then, add dose and be about 10～50mg/L; Add the PAM coagulant aids again, add dose and be about 1～5mg/L;
Said air-floating apparatus adopts the flat flow pressure air-dissolving air-float, and when air supporting was handled, effectively the residence time was 1～2h, and the dissolved air water reflux ratio is 20～30%;
3) filter:
Through the water after the air supporting processing, remove remaining aluminium through two medium mechanical filters again, the content that makes aluminium in the water is less than 0.3mg/L, and said mechanical filter adopts hard coal and silica sand as filtrate;
4) IX:
After water after filtering got into cation exchanger, removing carbon dioxide device, anion exchanger and mixed ion exchanger successively, water outlet was as power-plant makeup.
The step 2 of above-described water treatment method) in, the flow of dose through the pH value variable frequency adjustment hydrochloric acid dosing pump of the pH table feedback of dosing point outlet that add of hydrochloric acid reaches the purpose that adjusting hydrochloric acid adds dose; The dose that adds of PAC flocculation agent or oxalic acid is the flow that carries out the variable frequency adjustment dosing pump according to the signal of the feedback of the under meter on the pipeline; The dose that adds of PAM coagulant aids also is to come variable frequency adjustment to add dose according to the under meter feedback signal.
And step 2) in, air-floating apparatus adopts flat flow pressure air-dissolving shallow air-floatation equipment, makes molten gas bubble diameter be reduced to 50 μ m from 500 μ m.
Further; The present invention provides a kind of device of realizing above water treatment method; Comprise first lift pump, aeration tank, air-floating apparatus, buffer tank, second lift pump, fiber bundle filter, two medium filter, backwash water tank, the 3rd lift pump and ion exchange treatment system; The said first lifting pump intake is the inlet of aluminum oxide secondary condensed water; The water outlet of first lift pump is connected with the water inlet of aeration tank through pipeline; The water outlet of aeration tank is connected with the water-in of air-floating apparatus through pipeline, and the water outlet of air-floating apparatus is connected with the upper end water-in of buffer tank through pipeline, and the lower end water outlet of buffer tank promotes pump intake through pipeline second and connects; The water outlet of second lift pump through pipeline be connected respectively to, the water-in of fiber bundle filter and two medium filters; The water outlet of fiber bundle filter and two medium filters feeds in the backwash water tank through pipeline, and the said the 3rd promotes pump intake feeds the backwash water tank bottom through pipeline, and the water outlet of the 3rd lift pump is connected through the water-in of pipeline with the ion exchange treatment system; Be connected with three parallel dosing pumps on the pipeline between the water outlet of aeration tank and the water-in of air-floating apparatus, the rear pipeline of three dosing pumps is provided with mixing tank.
Further, more than ion exchange treatment system described in the device comprises cation exchanger, anion exchanger, mixed ion exchanger, carbon dioxide cleaner, acid regeneration case, sweet-water tank and alkali regeneration case; The 3rd lift pump is sent the water in the backwash water tank into cation exchanger and is carried out getting in the carbon dioxide cleaner after the cationic exchange again and handle; Water after being handled by carbon dioxide cleaner is sent into through water pump and is carried out anionresin in the anion exchanger, gets into mixed ion exchanger by the water after the anionresin; Said acid regeneration case is connected with the bottom of cation exchanger and mixed ion exchanger respectively with pipeline through the acid regeneration pump; Said sweet-water tank is connected with cation exchanger, anion exchanger and mixed ion exchanger respectively with pipeline through the desalination water pump; Said alkali regeneration case is connected with the bottom of anion exchanger and mixed ion exchanger respectively with pipeline through the alkali regenerative pump.
Above-mentioned air-floating apparatus comprises body water tank, slag scraper, dissolving, air compressor machine and air dissolved pump; Said slag scraper is located at the upper end of body water tank, and the bottom of body water tank is connected with the top of dissolving with pipeline through air dissolved pump, and dissolving also connects with the air outlet of air compressor machine through pipeline and is connected.
Be provided with coil heat exchanger in the above-mentioned aeration tank.
There is the water-in of backwash water pump the bottom of above-mentioned backwash water tank through pipe connection, and the water outlet of backwash water pump is connected with the bottom of fiber bundle filter with pair medium filters respectively through pipeline.
In the said apparatus, the medium of two medium filters is silica sand and hard coal, and silica sand and anthracitic thickness are 400mm.
The present invention has following beneficial effect:
The present invention adopts hydrochloric acid to regulate pH value when removing the aluminum oxide secondary condensed water, adds PAC flocculation agent or oxalic acid and PAM coagulant aids again, and the drug-treated of its interpolation is effective, and reaction product is nontoxic, need not carry out secondary treatment; Processing costs is rationally economical, and medicament, technology mode are easy to realize; Be used to realize the device good operation performance of water treatment method of the present invention, resistance to overload shock also can adapt to after the load variations and keep reliable effect.After the process air-floating apparatus is tentatively removed aluminium, remove remaining aluminium through two medium mechanical filters again.Mechanical filter adopts hard coal and silica sand as filtrate, can remove the most aluminium that pass through in the water of air-floating apparatus, makes that the content of aluminium is less than the standard of 0.3mg/L in the water, thereby avoids the aluminium too high levels that follow-up ion exchange resin is polluted.The aluminium content of filter back water is less than 0.3mg/L; Get into cation exchanger, removing carbon dioxide device, anion exchanger and mixed ion exchanger successively; Water outlet is as the supplementary feed of high-duty boiler, and the water after this apparatus processes meets the supply water supply standard of high-duty boiler fully.
Description of drawings
Fig. 1 connects synoptic diagram for the present invention realizes the device of water treatment method.
Wherein: 1 is first lift pump; 2 is the aeration tank; 3 is air-floating apparatus; 4 is buffer tank; 5 is second lift pump; 6 is fiber bundle filter; 7 is two medium filters; 8 is the ion exchange treatment system; 9 is coil heat exchanger; 10 is slag scraper; 11 is mixing tank; 12 is dissolving; 13 is air dissolved pump; 14 is air compressor machine; 15 are the backwash water tank; 16 is cation exchanger; 17 is anion exchanger; 18 is mixed ion exchanger; 19 is the 3rd lift pump; 20 is the body water tank; 21 is dosing pump; 22 is carbon dioxide cleaner; 23 is the acid regeneration case; 24 is sweet-water tank; 25 are alkali regeneration case; 26 is the acid regeneration pump; 27 is the desalination water pump; 28 is the alkali regenerative pump; 29 are the backwash water pump.
Embodiment
Describe in further detail as the device of the water treatment method of power-plant makeup realizing aluminum oxide secondary condensed water of the present invention below in conjunction with accompanying drawing:
Referring to Fig. 1, this device comprises first lift pump 1, aeration tank 2, air-floating apparatus 3, buffer tank 4, second lift pump 5, fiber bundle filter 6, two medium filter 7, backwash water tank 15, the 3rd lift pump 19 and ion exchange treatment system 8.The suction port of first lift pump 1 is the inlet of aluminum oxide secondary condensed water; The water outlet of first lift pump 1 is connected with the water inlet of aeration tank 2 through pipeline; The water outlet of aeration tank 2 is connected with the water-in of air-floating apparatus 3 through pipeline; The water outlet of air-floating apparatus 3 is connected with the upper end water-in of buffer tank 4 through pipeline; The suction port of the lower end water outlet of buffer tank 4 through pipeline second lift pump 5 connects, the water outlet of second lift pump 5 through pipeline be connected respectively to, the water-in of fiber bundle filter 6 and two medium filter 7, the water outlet of fiber bundle filter 6 and two medium filters 7 feeds in the backwash water tank 15 through pipeline; The suction port of said the 3rd lift pump 19 feeds backwash water tank 15 bottoms through pipeline, and the water outlet of the 3rd lift pump 19 is connected through the water-in of pipeline with ion exchange treatment system 8.The water-in of backwash water pump 29 is arranged through pipe connection at the bottom of said backwash water tank 15; The water outlet of backwash water pump 29 is connected with the bottom of fiber bundle filter 6 with two medium filters 7 respectively through pipeline; Wherein the medium of two medium filters 7 is silica sand and hard coal, and silica sand and anthracitic thickness are 400mm.Be provided with coil heat exchanger 9 in the aeration tank 2 of this device.The rear pipeline that is connected with 21, three dosing pumps 21 of three parallel dosing pumps on the pipeline between the water-in of the water outlet of aeration tank 2 and air-floating apparatus 3 is provided with mixing tank 11.
Above air-floating apparatus 3 comprises body water tank 20, slag scraper 10, dissolving 12, air compressor machine 14 and air dissolved pump 13; Slag scraper 10 is located at the upper end of body water tank 20, and the bottom of body water tank 20 is connected with the top of pipeline with dissolving 12 through air dissolved pump 13, and dissolving 12 also connects with the air outlet of air compressor machine 14 through pipeline and is connected.
The concrete structure of the ion exchange treatment system 8 of this device is such: it comprises cation exchanger 16, anion exchanger 17, mixed ion exchanger 18, carbon dioxide cleaner 22, acid regeneration case 23, sweet-water tank 24 and alkali regeneration case 25.The 3rd lift pump 19 is sent the water in the backwash water tank 15 into cation exchanger 16 and is carried out getting into processing in the carbon dioxide cleaner 22 again after the cationic exchange; Water after being handled by carbon dioxide cleaner 22 is sent into through water pump and is carried out anionresin in the anion exchanger 17, gets into mixed ion exchanger 18 by the water after the anionresin; Acid regeneration case 23 is connected with the bottom of cation exchanger 16 with mixed ion exchanger 18 respectively with pipeline through acid regeneration pump 26; Sweet-water tank 24 is connected with cation exchanger 16, anion exchanger 17 and mixed ion exchanger 18 respectively with pipeline through desalination water pump 27; Alkali regeneration case 25 is connected with the bottom of anion exchanger 17 with mixed ion exchanger 18 respectively with pipeline through alkali regenerative pump 28.
Technical process:
The flow process that adopts above device to carry out water technology is: alumina producer comes time condensation water (65～75 ℃ of water temperatures) after surface-type heat exchanger heat exchange to 35 ℃, sends into aeration tank 2 by first lift pump 1 and carries out aeration, and aeration rate designs by GWR at 7: 1.Aeration system can be removed the organism in the water of condensation.Water behind the aeration is through carrying out the air supporting processing from flowing into air-floating apparatus 3.On the inlet tube of air flotation device 3, add salt acid for adjusting pH value to 6～8 respectively successively, add flocculation agent PAC or oxalic acid then, add dose and be about 10～50mg/L, add coagulant aids PAM, add dose and be about 1～5mg/L.Water behind the aeration is through adding hydrochloric acid, flocculation agent (PAC or oxalic acid) and coagulant aids (PAM) and fully getting into air-floating apparatus 3 after the reaction; Air-floating apparatus 3 adopts the flat flow pressure air-dissolving air-float; The parameter that air supporting is handled is effective residence time: 1～2h, dissolved air water reflux ratio: 20～30%.This process using flat flow pressure air-dissolving shallow air-floatation equipment uses efficient reliever, makes molten gas bubble diameter be reduced to 50 μ m from 500 μ m, thereby has further improved clearance, has guaranteed removal effect.Air-float technology can reach 50%～60% to the clearance of aluminium.
Behind air-floating apparatus 3 preliminary removal aluminium, remove remaining aluminium through two medium filters 7 again.Two medium filters 7 can be removed through the most aluminium in the water of air-floating apparatus 3, make that the content of aluminium is less than the standard of 0.3mg/L in the water, thereby avoid the aluminium too high levels that follow-up ion exchange resin is polluted.
The aluminium content of filter back water gets into cation exchanger 16, carbon dioxide cleaner 22, anion exchanger 17 and mixed ion exchanger 18 successively less than 0.3mg/L, and the water outlet of mixed ion exchanger 18 is as the supplementary feed of high-duty boiler.
Below in conjunction with embodiment the water treatment method of aluminum oxide secondary condensed water of the present invention as power-plant makeup specifically described, following examples all adopt the device among above-mentioned Fig. 1 to realize.
Embodiment 1
Specifically may further comprise the steps of present embodiment:
1) cooling, degradation of contaminant: the time condensation water that alumina producer is come feeds the aeration tank and carries out aeration after surface-type heat exchanger heat exchange to 35 ℃, and the GWR of aeration is 7: 1;
2) flocculation, air supporting: the water behind the aeration gets into air-floating apparatus through pipeline self and carries out the air supporting processing; On the inlet tube of air-floating apparatus, at first add hydrochloric acid and regulate the pH value to 7.0 of water, add the PAC flocculation agent then, add dose and be about 10mg/L; Add the PAM coagulant aids again, add dose and be about 1mg/L; Said air-floating apparatus adopts the flat flow pressure air-dissolving air-float, and when air supporting was handled, effectively the residence time was 1.5h, and the dissolved air water reflux ratio is 20%; The flow of dose through the pH value variable frequency adjustment hydrochloric acid dosing pump of the pH table feedback of dosing point outlet that add of hydrochloric acid reaches the purpose that adjusting hydrochloric acid adds dose; The dose that adds of PAC flocculation agent is the flow that carries out the variable frequency adjustment dosing pump according to the signal of the feedback of the under meter on the pipeline; The dose that adds of PAM coagulant aids also is to come variable frequency adjustment to add dose according to the under meter feedback signal.Air-floating apparatus adopts flat flow pressure air-dissolving shallow air-floatation equipment, makes molten gas bubble diameter be reduced to 50 μ m from 500 μ m.
3) filter: the water after handling through air supporting, remove remaining aluminium through two medium mechanical filters again, the content that makes aluminium in the water is less than 0.3mg/L, and said mechanical filter adopts hard coal and silica sand as filtrate;
4) IX: after water after filtering got into cation exchanger, removing carbon dioxide device, anion exchanger and mixed ion exchanger successively, water outlet was as power-plant makeup.
Specifically may further comprise the steps of present embodiment:
1) cooling, degradation of contaminant: the time condensation water that alumina producer is come feeds the aeration tank and carries out aeration after surface-type heat exchanger heat exchange to 35 ℃, and the GWR of aeration is 7: 1;
2) flocculation, air supporting: the water behind the aeration gets into air-floating apparatus through pipeline self and carries out the air supporting processing; On the inlet tube of air-floating apparatus, at first add hydrochloric acid and regulate the pH value to 7.3 of water; Add the PAC flocculation agent then; Add dose and be about 20mg/L, add the PAM coagulant aids again, add dose and be about 1.5mg/L; Said air-floating apparatus adopts the flat flow pressure air-dissolving air-float, and when air supporting was handled, effectively the residence time was 1.5h, and the dissolved air water reflux ratio is 25%; The flow of dose through the pH value variable frequency adjustment hydrochloric acid dosing pump of the pH table feedback of dosing point outlet that add of hydrochloric acid reaches the purpose that adjusting hydrochloric acid adds dose; The dose that adds of PAC flocculation agent is the flow that carries out the variable frequency adjustment dosing pump according to the signal of the feedback of the under meter on the pipeline; The dose that adds of PAM coagulant aids also is to come variable frequency adjustment to add dose according to the under meter feedback signal.Air-floating apparatus adopts flat flow pressure air-dissolving shallow air-floatation equipment, makes molten gas bubble diameter be reduced to 50 μ m from 500 μ m.
3) filter: the water after handling through air supporting, remove remaining aluminium through two medium mechanical filters again, the content that makes aluminium in the water is less than 0.3mg/L, and said mechanical filter adopts hard coal and silica sand as filtrate;
4) IX: after water after filtering got into cation exchanger, removing carbon dioxide device, anion exchanger and mixed ion exchanger successively, water outlet was as power-plant makeup.
Embodiment 3
Specifically may further comprise the steps of present embodiment:
1) cooling, degradation of contaminant: the time condensation water that alumina producer is come feeds the aeration tank and carries out aeration after surface-type heat exchanger heat exchange to 35 ℃, and the GWR of aeration is 7: 1;
2) flocculation, air supporting: the water behind the aeration gets into air-floating apparatus through pipeline self and carries out the air supporting processing; On the inlet tube of air-floating apparatus, at first add hydrochloric acid and regulate the pH value to 7.5 of water, add oxalic acid then, add dose and be about 30mg/L; Add the PAM coagulant aids again, add dose and be about 2mg/L; Said air-floating apparatus adopts the flat flow pressure air-dissolving air-float, and when air supporting was handled, effectively the residence time was 1.5h, and the dissolved air water reflux ratio is 30%; The flow of dose through the pH value variable frequency adjustment hydrochloric acid dosing pump of the pH table feedback of dosing point outlet that add of hydrochloric acid reaches the purpose that adjusting hydrochloric acid adds dose; The dose that adds of oxalic acid is the flow that carries out the variable frequency adjustment dosing pump according to the signal of the feedback of the under meter on the pipeline; The dose that adds of PAM coagulant aids also is to come variable frequency adjustment to add dose according to the under meter feedback signal.Air-floating apparatus adopts flat flow pressure air-dissolving shallow air-floatation equipment, makes molten gas bubble diameter be reduced to 50 μ m from 500 μ m.
3) filter: the water after handling through air supporting, remove remaining aluminium through two medium mechanical filters again, the content that makes aluminium in the water is less than 0.3mg/L, and said mechanical filter adopts hard coal and silica sand as filtrate;
4) IX: after water after filtering got into cation exchanger, removing carbon dioxide device, anion exchanger and mixed ion exchanger successively, water outlet was as power-plant makeup.
Embodiment 4
Specifically may further comprise the steps of present embodiment:
1) cooling, degradation of contaminant: the time condensation water that alumina producer is come feeds the aeration tank and carries out aeration after surface-type heat exchanger heat exchange to 35 ℃, and the GWR of aeration is 7: 1;
2) flocculation, air supporting: the water behind the aeration gets into air-floating apparatus through pipeline self and carries out the air supporting processing; On the inlet tube of air-floating apparatus, at first add hydrochloric acid and regulate the pH value to 7.5 of water, add oxalic acid then, add dose and be about 50mg/L; Add the PAM coagulant aids again, add dose and be about 5mg/L; Said air-floating apparatus adopts the flat flow pressure air-dissolving air-float, and when air supporting was handled, effectively the residence time was 1.5h, and the dissolved air water reflux ratio is 30%; The flow of dose through the pH value variable frequency adjustment hydrochloric acid dosing pump of the pH table feedback of dosing point outlet that add of hydrochloric acid reaches the purpose that adjusting hydrochloric acid adds dose; The dose that adds of oxalic acid is the flow that carries out the variable frequency adjustment dosing pump according to the signal of the feedback of the under meter on the pipeline; The dose that adds of PAM coagulant aids also is to come variable frequency adjustment to add dose according to the under meter feedback signal.Air-floating apparatus adopts flat flow pressure air-dissolving shallow air-floatation equipment, makes molten gas bubble diameter be reduced to 50 μ m from 500 μ m.
3) filter: the water after handling through air supporting, remove remaining aluminium through two medium mechanical filters again, the content that makes aluminium in the water is less than 0.3mg/L, and said mechanical filter adopts hard coal and silica sand as filtrate;
4) IX: after water after filtering got into cation exchanger, removing carbon dioxide device, anion exchanger and mixed ion exchanger successively, water outlet was as power-plant makeup.
Claims (10)
1. an aluminum oxide secondary condensed water is characterized in that as the water treatment method of power-plant makeup, may further comprise the steps:
1) cooling, degradation of contaminant:
The time condensation water that alumina producer is next feeds the aeration tank and carries out aeration after the surface-type heat exchanger heat exchange;
2) flocculation, air supporting:
Water behind the aeration gets into air-floating apparatus through pipeline self and carries out the air supporting processing; On the inlet tube of air-floating apparatus, at first add hydrochloric acid and regulate pH value to 6～8 of water, add PAC flocculation agent or oxalic acid then, adding dose is 10～50mg/L; Add the PAM coagulant aids again, adding dose is 1～5mg/L;
Said air-floating apparatus adopts the flat flow pressure air-dissolving air-float, and when air supporting was handled, effectively the residence time was 1～2h, and the dissolved air water reflux ratio is 20～30%;
3) filter:
Through the water after the air supporting processing, remove remaining aluminium through two medium mechanical filters again, the content that makes aluminium in the water is less than 0.3mg/L, and said mechanical filter adopts hard coal and silica sand as filtrate;
4) IX:
After water after filtering got into cation exchanger, removing carbon dioxide device, anion exchanger and mixed ion exchanger successively, water outlet was as power-plant makeup.
2. aluminum oxide secondary condensed water according to claim 1 is characterized in that as the water treatment method of power-plant makeup, and in the step 1), time condensation water is through surface-type heat exchanger heat exchange to 35 ℃; The GWR of aeration is 7: 1.
3. aluminum oxide secondary condensed water according to claim 1 is as the water treatment method of power-plant makeup; It is characterized in that; Step 2) in, the flow of dose through the pH value variable frequency adjustment hydrochloric acid dosing pump of the pH table feedback of dosing point outlet that add of hydrochloric acid reaches the purpose that adjusting hydrochloric acid adds dose; The dose that adds of PAC flocculation agent or oxalic acid is the flow that carries out the variable frequency adjustment dosing pump according to the signal of the feedback of the under meter on the pipeline; The dose that adds of PAM coagulant aids also is to come variable frequency adjustment to add dose according to the under meter feedback signal.
4. aluminum oxide secondary condensed water according to claim 1 is characterized in that step 2 as the water treatment method of power-plant makeup) in, air-floating apparatus adopts flat flow pressure air-dissolving shallow air-floatation equipment, makes molten gas bubble diameter be reduced to 50 μ m from 500 μ m.
5. device of realizing the said water treatment method of claim 1; Comprise first lift pump (1), aeration tank (2), air-floating apparatus (3), buffer tank (4), second lift pump (5), fiber bundle filter (6), two medium filter (7), backwash water tank (15), the 3rd lift pump (19) and ion exchange treatment system (8); It is characterized in that; The suction port of said first lift pump (1) is the inlet of aluminum oxide secondary condensed water; The water outlet of first lift pump (1) is connected with the water inlet of aeration tank (2) through pipeline; The water outlet of aeration tank (2) is connected with the water-in of air-floating apparatus (3) through pipeline; The water outlet of air-floating apparatus (3) is connected through the upper end water-in of pipeline with buffer tank (4); The suction port of the lower end water outlet of buffer tank (4) through pipeline second lift pump (5) connects, and the water outlet of second lift pump (5) is connected respectively to the water-in of fiber bundle filter (6) and two medium filters (7) through pipeline, and the water outlet of fiber bundle filter (6) and two medium filters (7) passes through in the pipeline feeding backwash water tank (15); The suction port of said the 3rd lift pump (19) feeds backwash water tank (15) bottom through pipeline, and the water outlet of the 3rd lift pump (19) is connected through the water-in of pipeline with ion exchange treatment system (8); Be connected with three parallel dosing pumps (21) on the pipeline between the water-in of the water outlet of aeration tank (2) and air-floating apparatus (3), the rear pipeline of three dosing pumps (21) is provided with mixing tank (11).
6. device according to claim 5; It is characterized in that said ion exchange treatment system (8) comprises cation exchanger (16), anion exchanger (17), mixed ion exchanger (18), carbon dioxide cleaner (22), acid regeneration case (23), sweet-water tank (24) and alkali regeneration case (25); The 3rd lift pump (19) is sent the water in the backwash water tank (15) into cation exchanger (16) and is carried out getting into processing in the carbon dioxide cleaner (22) again after the cationic exchange; Water after being handled by carbon dioxide cleaner (22) is sent in the anion exchanger (17) through water pump and is carried out anionresin, gets into mixed ion exchanger (18) by the water after the anionresin; Said acid regeneration case (23) is connected with the bottom of cation exchanger (16) with mixed ion exchanger (18) respectively with pipeline through acid regeneration pump (26); Said sweet-water tank (24) is connected with cation exchanger (16), anion exchanger (17) and mixed ion exchanger (18) respectively with pipeline through desalination water pump (27); Said alkali regeneration case (25) is connected with the bottom of anion exchanger (17) with mixed ion exchanger (18) respectively with pipeline through alkali regenerative pump (28).
7. device according to claim 5 is characterized in that, said air-floating apparatus (3) comprises body water tank (20), slag scraper (10), dissolving (12), air compressor machine (14) and air dissolved pump (13); Said slag scraper (10) is located at the upper end of body water tank (20), and the bottom of body water tank (20) is connected with the top of pipeline with dissolving (12) through air dissolved pump (13), and dissolving (12) also is connected with the air outlet of air compressor machine (14) through pipeline.
8. device according to claim 5 is characterized in that, is provided with coil heat exchanger (9) in said aeration tank (2).
9. device according to claim 5; It is characterized in that; There is the water-in of backwash water pump (29) bottom of said backwash water tank (15) through pipe connection, and the water outlet of backwash water pump (29) is connected with the bottom of fiber bundle filter (6) with pair medium filters (7) respectively through pipeline.
10. device according to claim 5 is characterized in that, the medium of said pair of medium filter (7) is silica sand and hard coal, and silica sand and anthracitic thickness are 400mm.
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| CN103739115A (en) * | 2013-12-27 | 2014-04-23 | 陕西大唐新能电力设计有限公司 | Station boiler make-up water treatment method |
| CN104006373A (en) * | 2014-05-30 | 2014-08-27 | 上海汇闵能源科技有限公司 | Device and method for recycling afterheat of smoke of steam boiler |
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