CN204310904U - A kind of system reclaiming salt from Waste Water Treatment - Google Patents
A kind of system reclaiming salt from Waste Water Treatment Download PDFInfo
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- CN204310904U CN204310904U CN201420622932.5U CN201420622932U CN204310904U CN 204310904 U CN204310904 U CN 204310904U CN 201420622932 U CN201420622932 U CN 201420622932U CN 204310904 U CN204310904 U CN 204310904U
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Abstract
The utility model discloses a kind of system reclaiming salt from Waste Water Treatment, by wastewater streams to comprising COD unit, decon and scale-forming ion unit, PH regulon, membrane concentration unit, two sections of crystalline elements, first degree crystalline separating unit, secondary freezing and crystallizing unit, single-action or multiple-effect evaporation unit, three grades of crystalline elements and mother liquor ponds successively.The system reclaiming salt from Waste Water Treatment described in the utility model, by being oxidized, adsorbing, precipitate, filter, soften, go the processing steps such as CO2 to waste water, waste water is processed, remove relevant ions and impurity, get rid of the speed that affects on RO reverse osmosis and effect, guarantee the purity of nitre and the salt extracted simultaneously; In system, energy conversion unit is set, the heat of first degree crystalline separating unit, secondary freezing and crystallizing unit and single-action or multiple-effect evaporation unit, three grades of crystalline elements is mutually transformed and uses, improve energy utilization rate, to greatest extent saving resource.
Description
Technical field
The utility model relates to a kind of system reclaiming salt from Waste Water Treatment, can isolate industrial salt and purify, be specially adapted to the process of coal chemical industry sewage, belong to energy-saving and emission-reduction and waste reclaimation field while the objectionable impurities in waste water being removed.
Background technology
Along with the continuous construction of industrial installation, its sewage, waste gas, waste discharge amount also constantly increase, environment tolerance and discharge permit amount also more and more less, so Zero discharging system is also in continuous popularization.In large Industrial processes, the requirement of zero release is also more and more higher, such as build the mega project such as more than 1,000,000 tons methyl alcohol and attached coal acetic acid, ethylene glycol, olefin hydrocarbon making by coal, if implementation zero release, energy-saving and emission-reduction will be realized to greatest extent, but meanwhile, 2-5 ten thousand tons of abraum salts will be produced every year.It will be higher for discharging abraum salt amount every year for the area that saltiness in water-deficient area, northwest or former water is high, how to process these abraum salts and annoying numerous engineering technical personnel always, especially for solubility abraum salt, though can be given up degree to non-danger by the process of technical finesse means, but its final intractability is very large, can not landfill, also can not use.Therefore find a kind of resource utilization method to seem particularly important, the utility model object will overcome the above problems exactly.
Through retrieval, apply for " zero release " Patents 795 in recent years, as CN103253820B " Efficient liquid zero-discharge wastewater treatment method and system ", CN10328809A " a kind for the treatment of process of coal gasification waste water zero release, treatment system and application ", CN103319042A " the complicated waste water recycling of high salt and zero release integrated equipment and technique " etc.Meanwhile, we have also searched for " reclaiming salt method or solventing-out " Patents, but recycle for the purification of the crystal salt in sewage zero-discharge, and involved patent is little.Because the salt in trade effluent contains a large amount of COD or carnallite existence, or normally by concentrating the crystal salt formed in former water step by step later, and also contain other ions as Ca
2 +, Mg
2 +, K
+, NO
3 -, HCO
3 -deng impact, the difficulty that single salt reclaims is very large, is difficult to meet make isolated salt reach the standard of industrial salt.At present, the resource utilization method of this class and device also do not have.
General sal prunella technique Crystallization Separation is applicable in waste water containing Na
2sO
4time lower, usual employing quadruple effect, five effect or MVR carry out fractional crystallization, its Tc is selected in 50 ~ 120 DEG C, is namely first evaporated at a lower temperature by bittern, while NaCl separates out in a large number, Na
2sO
4being concentrated, being had Na at it close to heating up time saturated
2sO
4separate out to reach solventing-out.The feature of this technique is by sal prunella Brine salinity about 93% ~ 98%, and bittern concentration is comparatively large, and water ratio is lower.And working condition requires harsh, is embodied in:
1. pair former quality requires high, and sodium sulphate content needs strict to control and constant, generally 3 ~ 10%, when sulfate mono sodium content is higher, separating technology more complicated, needs repeatedly to regulate temperature and waste strength to be separated different salt, and the salt reclaimed is impure, containing more impurity;
2. water, electricity, vapour and temperature control requirement are high to external world, if a certain condition changes, separating-purifying just may be caused uneven;
3. operate, adjustment difficulty is large and vaporization heat efficiency has room for promotion, causes wasting of resources cost to increase.
Utility model content
Utility model object: what the purpose of this utility model was to provide a kind of practicality is applicable to large industrial production, particularly petrochemical complex, Coal Chemical Industry etc. produce after the system reclaiming salt from Waste Water Treatment.This system practical simplicity, the saving energy, the main precipitation salt after being simultaneously separated can reach industrial grade III Standard or higher standard, really realizes commercialization and recycling, effectively can utilize the energy transformation in each step simultaneously.。
Technical scheme: the system reclaiming salt from Waste Water Treatment described in the utility model, its objective is and like this to realize:
A kind of system reclaiming salt from Waste Water Treatment, by wastewater streams to comprising COD unit, decon and scale-forming ion unit, PH regulon, membrane concentration unit, two sections of crystalline elements, first degree crystalline separating unit, secondary freezing and crystallizing unit, single-action or multiple-effect evaporation unit, three grades of crystalline elements and mother liquor ponds successively
Described decon and scale-forming ion unit comprise the lime settling pond, multistage filter, water softening device, the carbonic acid gas carbon removal device that are communicated with successively;
Described PH regulon is PH equalizing tank;
Described membrane concentration unit is secondary RO system;
Described two sections of crystalline elements are two sections of MVR vaporizers;
Described first degree crystalline separating unit comprises thickener, the first whizzer;
Secondary freezing and crystallizing unit comprises freezing and crystallizing device, the second whizzer;
Described single-action or multiple-effect evaporation unit comprise single-action or multiple-effect evaporator;
Described three grades of crystalline elements comprise freezing and crystallizing device, the 3rd whizzer.
System as above, just upgrading unit is also provided with between described membrane concentration unit and two sections of crystalline elements, described just upgrading unit comprises one section of MVR vaporizer, it is concentrated that high TDS waste water after membrane concentration unit R O reverse osmosis concentration carries out tentatively compared with big yield by first upgrading unit, then enters the follow-up process analysed nitre and analyse salt.
System as above, described mother liquor pond is also provided with water outlet branch road and is communicated with first upgrading unit, and water outlet branch road is provided with interchanger, and waste liquid enters just upgrading unit after flowing through interchanger preheating by water outlet branch road, mix with the waste water in first upgrading unit, again participate in the process analysed nitre and analyse salt.
System as above, energy conversion unit is provided with between described second stage freezing and crystallizing unit and single-action or multiple-effect evaporation unit, described energy conversion unit comprises heat pump and interchanger, interchanger is located between single-action in the second whizzer in secondary freezing and crystallizing unit and single-action or multiple-effect evaporation unit or multiple-effect evaporator, heat pump connects freezing and crystallizing device and interchanger, the heat of first degree crystalline separating unit, secondary freezing and crystallizing unit and single-action or multiple-effect evaporation unit, three grades of crystalline elements is mutually transformed and uses, improves energy utilization rate.
Utilize said system, from Waste Water Treatment, reclaim salt by following processing step and purify, specific as follows:
(1) strong oxidizer is added in waste water;
(2) waste water is by removing COD unit, removes film Scale inhibitors and the NH of oxidized organic pollutant and nitrite, sulfide, ferrous salt and remnants
4-N etc.;
(3) waste water is by clarification Calcified pond, removes HCO
3-;
(4) waste water is through cascade filtration process, removes suspended substance and throw out;
(5) waste water is through secondary softening removal hardness and basicity, and through carbonic acid gas carbon removal device, removes the carbonic acid gas in water;
(6) enter secondary RO system after waste water adjustment PH, carry out reverse osmosis concentration, make the TDS concentration of high-salt wastewater reach 30000 ~ 60000;
(7) waste water enters vaporizer and evaporates, and control temperature is at 75 ~ 100 DEG C, and concentrated post crystallization goes out Na
2sO
4;
(8) supersaturation waste water solution enters thickener, relies on cold water to control, makes temperature reach 50 ~ 100 DEG C, continue crystallization Na
2sO
4, obtain by centrifugation or filtration the industrial nitre meeting or exceeding industrial grade III Standard;
(9) waste water enters freezing and crystallizing device, relies on refrigerated water to control freezing, makes temperature reach 0 ~ 10 DEG C, and freezing and crystallizing separates out Na
2sO
4, obtain by centrifugation or filtration the industrial nitre meeting or exceeding industrial grade III Standard;
(10) analyse the later wastewater mother liquor of nitre and adopt single-action or multiple-effect evaporation, control temperature is at 50 ~ 120 DEG C, and concentrated precipitation NaCl, is arrived by centrifugation or filtration or exceed the Industrial Salt of industrial grade III Standard further;
(11) last wastewater mother liquor enters to mix with pending waste water in the vaporizer in step (7) and again evaporates, circulation step (7) ~ (10).
Consider that need waste water saltiness to be processed is relatively low, generally between 1% ~ 5%, water ratio is high, and the complicated component simultaneously, for common coal chemical industry sewage zero release, in waste water, the main component of salt is NaCl and Na
2sO
4, and both ratios are substantially at about 1:1, are difficult to NaCl and Na by general solventing-out technique
2sO
4separate and ensure purity, and COD and foreign matter content high, in conjunction with the feature that the evaporation of haline water hot pump in low temp or MVR run, the problem needing low or difficulty crystallizes out to solubleness in evaporative process salt impurity, COD etc. to produce fouling or accumulation carries out preliminary treatment, remove reducing substances in water and impurity and scale-forming ion unit, the oxidation in the utility model step (1) ~ (5), absorption, precipitation, filtration, soften, remove CO
2namely be that preliminary treatment is carried out to waste water etc. technique, get rid of the speed that affects on RO reverse osmosis in step (6) and effect, guarantee the nitre of subsequent extracted and the purity of salt simultaneously, particularly in step (5), the effect of carbonic acid gas carbon removal device in ion exchange water treatment process is to remove the carbonic acid gas in water, alleviate the load of anionresin, improve economy and the effluent quality of water treatment system.
Beneficial effect: the system reclaiming salt from Waste Water Treatment described in the utility model, by being oxidized waste water, adsorbing, precipitate, filter, soften, remove CO
2deng processing step, waste water is processed, remove relevant ions and impurity, get rid of the speed that affects on RO reverse osmosis and effect, guarantee the purity of nitre and the salt extracted simultaneously, carbonic acid gas carbon removal device is particularly set, alleviate the load of anionresin, improve economy and the effluent quality of water treatment system; In system, energy conversion unit is set, the heat of first degree crystalline separating unit, secondary freezing and crystallizing unit and single-action or multiple-effect evaporation unit, three grades of crystalline elements is mutually transformed and uses, improve energy utilization rate, to greatest extent saving resource.
The utility model and traditional four-effect evaporation Energy-saving Situation is adopted to contrast as follows: with 100m
3/ h, the sewage of water inlet TDS 3.5% is example:
Note 1: for the sewage of 100t/h saliferous 3.5%wt in upper table;
Note 2: steam price 180 yuan/t, average electricity price 0.6 yuan/KWh, engineering cost depreciation in 14 years.
Accompanying drawing explanation
Fig. 1 is system architecture schematic diagram of the present utility model.
Wherein, in Fig. 1,1 is influent waste water; 2 for adding strong oxidizer; 3 for removing COD unit; 4 for adding Ca (OH)
2; 5 is clarification Calcified pond; 6 is multistage filter; 7 is water softening device; 8 is carbonic acid gas carbon removal device; 9 is PH equalizing tank; 10 is secondary RO system; 11 is one section of MVR vaporizer; 12 is two sections of MVR vaporizers; 13 is thickener; 14 is cooling circulating water; 15 is the first whizzer; 16 for going out nitre; 17 is freezing and crystallizing device; 18 is refrigerated water; 19 is the second whizzer; 20 for going out nitre; 21 is plate-type heat exchanger; 22 is heat pump; 23 is heat recirculated water; 24 is single-action or multiple-effect evaporator; 25 make a living steam; 26 is water of condensation; 27 is plate-type heat exchanger; 28 is cooling crystallizer; 29 is cooling circulating water; 30 is the 3rd whizzer; 31 for going out salt; 32 is mother liquor pond; 33 is activated carbon filtration; 34 is circulating water pool; 35 is biochemical system; 36 is settling tank; 37 is pressure filter; 38 is solid waste discharge; 39 is pollution discharge pond.
Embodiment
In order to deepen understanding of the present utility model, below in conjunction with embodiment and accompanying drawing, the utility model is described in further detail, and this embodiment, only for explaining the utility model, does not form the restriction to the utility model protection domain.
The shown in Figure 1 system architecture schematic diagram reclaiming salt from Waste Water Treatment, discloses specific embodiment of the present utility model as follows:
(1) waste water flows into system from influent waste water 1, adds strong oxidizer 2 and makes reducing substances oxidation in waste water;
(2) waste water is by removing COD unit 3, removes film Scale inhibitors and the NH of oxidized organic pollutant and nitrite, sulfide, ferrous salt and remnants
4-N etc., go to adopt in COD unit sorbing material to remove COD, and sorbing material is one or more in gac, coal ash, diatomite;
(3) waste water is by clarification Calcified pond 5, adopts and add Ca (OH) in pond
24 removing HCO
3-, its reaction is as follows:
Ca(OH)
2+HCO
3 -——CaCO
3↓+H
2O+OH
-；
(4) waste water processes through multistage filter 6, removes suspended substance and throw out;
(5) waste water is through water softening device secondary softening removal hardness and basicity, and through carbonic acid gas carbon removal device 8, removes the carbonic acid gas in water;
(6) waste water enters after PH equalizing tank 9 adjusts PH and enters secondary RO system 10, carries out reverse osmosis concentration, makes the TDS concentration of high-salt wastewater reach 30000 ~ 60000;
(7) waste water enters at the beginning of one section of MVR vaporizer 11 carries out and concentrates, and removes a large amount of water;
(8) waste water enters two sections of MVR vaporizers 12 and carries out two sections of crystallizations, and control temperature is at 75 ~ 100 DEG C, and concentrated post crystallization goes out Na
2sO
4;
(9) supersaturation waste water solution enters thickener 13, relies on cooling circulating water 14 to control, makes temperature reach 50 ~ 100 DEG C, continue crystallization Na
2sO
4, by going out the industrial nitre that nitre 16 obtains meeting or exceeding industrial grade III Standard after the first whizzer 15 centrifugation;
(10) waste water enters freezing and crystallizing device 17, and rely on refrigerated water 18 to control freezing, make temperature reach 0 ~ 10 DEG C, freezing and crystallizing goes out to analyse Na
2sO
4, by going out the industrial nitre that nitre 20 obtains meeting or exceeding industrial grade III Standard after the second whizzer 19 centrifugation;
(11) analyse the later wastewater mother liquor of nitre and enter single-action or multiple-effect evaporator 24 adopts single-action or multiple-effect evaporation, pass into raw steam 25, discharge water of condensation 26, control temperature is at 50 ~ 120 DEG C, concentrated precipitation NaCl further, enter cooling crystallizer 28 by cooling circulating water 29, by going out the Industrial Salt that salt 31 is arrived or exceedes industrial grade III Standard after the 3rd whizzer 30 centrifugation;
(12) wastewater mother liquor is reclaimed finally by mother liquor pond 32, mother liquor pond 32 is also provided with water outlet branch road and is communicated with one section of MVR vaporizer 11, water outlet branch road is provided with plate-type heat exchanger 27, wastewater mother liquor enters one section of MVR vaporizer 11 after flowing through plate-type heat exchanger 27 preheating by water outlet branch road, again mix with the waste water in first upgrading unit, again participate in the process analysed nitre and analyse salt, wherein plate-type heat exchanger 27 passes into raw steam 25, discharges water of condensation 26 and reaches heat transfer process.
Plate-type heat exchanger 21 is provided with between the second whizzer 19 and single-action or multiple-effect evaporator 24, plate-type heat exchanger 21 connects heat pump 22, heat pump 22 connects freezing and crystallizing device 17, the refrigerated water 18 of circulation is provided to freezing and crystallizing device 17, refrigerated water through freezing and crystallizing device 17 preheating is recycled to plate-type heat exchanger 21 through heat pump and carries out thermal exchange, and temperature continues to be circulated to freezing and crystallizing device 17 after reducing.Plate-type heat exchanger 21 and heat pump 22 form energy conversion unit, and the heat of first degree crystalline separating unit, secondary freezing and crystallizing unit and single-action or multiple-effect evaporation unit, three grades of crystalline elements is mutually transformed and used, and improve energy utilization rate.
Simultaneously, one section of MVR vaporizer 11 and two sections of MVR vaporizers 12 are also connected to circulating water pool 34 and biochemical system 35 simultaneously, in parallelly on pipeline between circulating water pool 34 with one section of MVR vaporizer 11, between circulating water pool 34 with two sections of MVR vaporizers 12 be provided with activated carbon filtration 33, simultaneously, secondary RO unit also connects circulating water pool 34, two sections of MVR vaporizers 12 also connect pollution discharge pond 39, at set intervals, two sections of MVR vaporizers 12 need to carry out blowdown, and the blowdown in pollution discharge pond 39 can reprocessing or take out after removing the organism such as COD further.
Clarification Calcified pond 5 connects settling tank 36, and settling tank 36 connects pressure filter 37, the precipitation in clarification Calcified pond 5 can be built up to settling tank 36, and process through pressure filter 37, be reclaimed by solid waste 38.
The method reclaiming salt from Waste Water Treatment described in the utility model, by the oxidation in step (1) ~ (5), absorption, precipitation, filtration, softens, removes CO
2deng processing step, waste water is processed, removal relevant ions and impurity eliminating are on the speed that affects of RO reverse osmosis in step (6) and effect, guarantee the purity of nitre that subsequent step (7) ~ (11) extract and salt simultaneously, particularly in step (5), except the carbonic acid gas in anhydrating, alleviate the load of anionresin, improve economy and the effluent quality of water treatment system; In the process of separating-purifying nitre and salt, by the research to temperature and solubleness relation, the substep proposing a set of intensification-cooling-intensification is analysed nitre, is analysed the technique of salt, guarantees that the nitre of extraction and salt meet purity requirement, the devil liquor recovery after process is carried out secondary treatment simultaneously.
The invention also discloses and utilize the above system reclaiming the technique of salt from Waste Water Treatment, in system, energy conversion unit is set, the heat of first degree crystalline separating unit, secondary freezing and crystallizing unit and single-action or multiple-effect evaporation unit, three grades of crystalline elements is mutually transformed and uses, improve energy utilization rate, to greatest extent saving resource.
It is below the water quality table through step (1) ~ (5) processed waste water
Note: total alkalinity is (with CaCO
3meter) (mg/L)
Total hardness is (with CaCO
3meter) (mg/L)
Estimation before vaporizer advancing water: NaCl:236.6* (35.5+23)=13841.7mg/L
Na
2SO
4：185.4/2*(46+96)＝13163.4mg/L
Can clearly find out in table, in waste water after treatment, COD content obviously reduces, the Ca contained
2+, M
g 2+, HCO
3 -ion substantially removes, and eliminates the follow-up impact of analysing nitre, analysing salt.
The foregoing is only preferred embodiment of the present utility model; not in order to limit the utility model; all within spirit of the present utility model and principle, any amendment done, equivalent replacement, improvement etc., all should be included within protection domain of the present utility model.
Claims (4)
1. one kind is reclaimed the system of salt from Waste Water Treatment, it is characterized in that, by wastewater streams to comprising COD unit, decon and scale-forming ion unit, PH regulon, membrane concentration unit, two sections of crystalline elements, first degree crystalline separating unit, secondary freezing and crystallizing unit, single-action or multiple-effect evaporation unit, three grades of crystalline elements and mother liquor ponds successively
Described decon and scale-forming ion unit comprise the lime settling pond, multistage filter, water softening device, the carbonic acid gas carbon removal device that are communicated with successively;
Described PH regulon is PH equalizing tank;
Described membrane concentration unit is secondary RO system;
Described two sections of crystalline elements are two sections of MVR vaporizers;
Described first degree crystalline separating unit comprises thickener, the first whizzer;
Secondary freezing and crystallizing unit comprises freezing and crystallizing device, the second whizzer;
Described single-action or multiple-effect evaporation unit comprise single-action or multiple-effect evaporator;
Described three grades of crystalline elements comprise freezing and crystallizing device, the 3rd whizzer.
2. the system reclaiming salt from Waste Water Treatment according to claim 1, is characterized in that, is also provided with just upgrading unit between described membrane concentration unit and two sections of crystalline elements, and described just upgrading unit comprises one section of MVR vaporizer.
3. the system reclaiming salt from Waste Water Treatment according to claim 2, is characterized in that, described mother liquor pond is also provided with water outlet branch road and is communicated with first upgrading unit, and waste water enters just upgrading unit after flowing through interchanger preheating by water outlet branch road.
4. according to the system reclaiming salt from Waste Water Treatment in claims 1 to 3 described in any one, it is characterized in that, energy conversion unit is provided with between described secondary freezing and crystallizing unit and single-action or multiple-effect evaporation unit, described energy conversion unit comprises heat pump and interchanger, interchanger is located between single-action in the second whizzer in secondary freezing and crystallizing unit and single-action or multiple-effect evaporation unit or multiple-effect evaporator, and heat pump connects freezing and crystallizing device and interchanger.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420622932.5U CN204310904U (en) | 2014-10-24 | 2014-10-24 | A kind of system reclaiming salt from Waste Water Treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420622932.5U CN204310904U (en) | 2014-10-24 | 2014-10-24 | A kind of system reclaiming salt from Waste Water Treatment |
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| Publication Number | Publication Date |
|---|---|
| CN204310904U true CN204310904U (en) | 2015-05-06 |
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ID=53133231
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104326612A (en) * | 2014-10-24 | 2015-02-04 | 南京科盛环保科技有限公司 | Method and system for recovering salt from waste water treatment system |
| CN105384295A (en) * | 2015-12-07 | 2016-03-09 | 江西省广德环保科技股份有限公司 | Zero-discharge processing method of high salinity wastewater |
| CN106276978A (en) * | 2016-08-03 | 2017-01-04 | 浙江海洋大学 | A kind of suction automatically receives salt dolly |
| CN110683604A (en) * | 2019-10-30 | 2020-01-14 | 徐州工程学院 | Waste water utilization and flue gas emission reduction system based on solar energy |
-
2014
- 2014-10-24 CN CN201420622932.5U patent/CN204310904U/en not_active Withdrawn - After Issue
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104326612A (en) * | 2014-10-24 | 2015-02-04 | 南京科盛环保科技有限公司 | Method and system for recovering salt from waste water treatment system |
| CN104326612B (en) * | 2014-10-24 | 2016-03-09 | 南京科盛环保科技有限公司 | A kind of method and system reclaiming salt from Waste Water Treatment |
| CN105384295A (en) * | 2015-12-07 | 2016-03-09 | 江西省广德环保科技股份有限公司 | Zero-discharge processing method of high salinity wastewater |
| CN106276978A (en) * | 2016-08-03 | 2017-01-04 | 浙江海洋大学 | A kind of suction automatically receives salt dolly |
| CN110683604A (en) * | 2019-10-30 | 2020-01-14 | 徐州工程学院 | Waste water utilization and flue gas emission reduction system based on solar energy |
| CN110683604B (en) * | 2019-10-30 | 2022-05-13 | 徐州工程学院 | Waste water utilization and flue gas emission reduction system based on solar energy |
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Granted publication date: 20150506 Effective date of abandoning: 20160309 |
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