CN206359377U - The special equipment of the separation of salt and crystallization process for reclaiming in brine waste - Google Patents
The special equipment of the separation of salt and crystallization process for reclaiming in brine waste Download PDFInfo
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- CN206359377U CN206359377U CN201621406066.1U CN201621406066U CN206359377U CN 206359377 U CN206359377 U CN 206359377U CN 201621406066 U CN201621406066 U CN 201621406066U CN 206359377 U CN206359377 U CN 206359377U
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Abstract
The special equipment of the separation of salt and crystallization process for reclaiming in brine waste, the sodium chloride in brine waste and sodium sulphate are separated by nanofiltration first, nanofiltration produces water and passes through oxidation, evaporative crystallization, it is dried to obtain sodium chloride product, nanofiltration concentrated water first passes through freezing and crystallizing and obtains sal glauberi crystal, then it is large grain anhydrous sodium sulfate product to melt large particle crystal by sal glauberi crystal transformation by salt again, avoid product salt fine size in single refrigeration crystallization process, dehydration is difficult, the problem of caking, reduce carnallite yield, reduce pollution, a large amount of carnallites are saved as the cost of fixed-end forces, and two kinds of sodium salt recyclings, economic value can be created.
Description
Technical field
The utility model belongs to technical field of waste water processing, be exactly specifically be related in a kind of brine waste the separation of salt and
Crystallize the special equipment of process for reclaiming.
Background technology
Increasingly attention with society to environmental protection, starts to be controlled total emission volumn, and general sewage passes through
The treatment technologies such as biology, chemistry can meet qualified discharge, still, the pillar industry such as petrochemical industry, coal chemical industry, electric power, mining
The a large amount of high-concentration salt-containing wastewaters produced, 75%~95% waste water can only be reclaimed by the conventional process such as biology, materialization means,
Remaining 5%~25% high-concentration salt-containing wastewater by concentration can not be utilized.At present, what in the market had is stored by exposure pond
Get up, such as run into mountain torrents, geology disaster, the brine waste of high concentration is once a leak occurs, by polluted surface, body of groundwater, endanger
Greatly.
The solid that wastewater zero discharge process is produced is generally carnallite, and security landfill processing is carried out usually as dangerous solid waste,
This mode not only needs auxiliary construction dangerous solid waste landfill site with high investment, and it is expensive to carry out processing cost；In addition, also needing
The waste water scratch pool of the big volume of auxiliary construction, the capacity of waste water scratch pool generally requires even nearly million cubic metres of hundreds of thousands, throws
Provide more than one hundred million members.Therefore, the handling problems of solid carnallite, are the main bugbears for hindering high-concentration salt-containing wastewater zero-discharge technology.
Freezing and crystallizing technology is that brine waste temperature is down into 0 DEG C or so by the method for freezing, according to someization in water
The big principle of sensitivity of the solubility of compound to temperature, a kind of technology of crystallization treatment is carried out to waste water.Due to normal in waste water
Change unconspicuous material containing some solubility with temperature, therefore, the centrifuge mother liquor of freezing and crystallizing technology is in freezing and crystallizing system
Part circulation is carried out in system, that is, needs to discharge a part of centrifuge mother liquor from system China and foreign countries, it is also one that how the mother liquor, which is effectively handled,
Individual problem.
At present, batch crystallization process account for more than 95% in industry in freezing and crystallizing, the poor product quality of the technique, comprehensive
High energy consumption is closed, corrosivity is big, plugging, caking phenomenon are protruded, but more major problem is that product salt fine size, dehydration are difficult,
Caking is serious, have impact on the quality of product salt.
Utility model content
The purpose of this utility model be directed in above-mentioned brine waste processing procedure the carnallite problem of producing, mother liquor problem, with
And the product granularity that freezing and crystallizing is obtained is thin, difficult problem is dehydrated, the utility model provides salt in a kind of brine waste
Separation and the special purpose device of crystallization process for reclaiming, can separate the sodium chloride in brine waste, sodium sulphate, and by mother
Liquid is converted into carnallite, not only reduces harm of the pollutant to environment, and the two kinds of salt separated from brine waste can
Recycling, creates economic value.
Technical scheme
In order to realize the separation of salt and crystallization process for reclaiming in above-mentioned technical purpose, the utility model design brine waste
Special equipment, it is characterised in that：It includes preatreating reactors, nano-filtration unit, the first oxidation reactor, evaporative crystallization system
System, the second oxidation reactor, freezing and crystallizing system, organic upgrading unit and salt melt crystal system；
Former pond is connected with preatreating reactors, and the first intake pump, the output of preatreating reactors are housed on connecting line
End connection nano-filtration unit, the production water output end of nano-filtration unit connects the first oxidation reactor, and the concentrated water output end of nano-filtration unit connects
Intermediate pool is connect, the output end connection evaporation and crystallization system of the first oxidation reactor, the crystal output end of evaporation and crystallization system connects
The first drier is connect, the mother liquor output end of evaporation and crystallization system connects the second drier, the output end connection chlorine of the first drier
Change sodium Product recycling bag, intermediate pool is connected with freezing and crystallizing system, and the second intake pump, freezing and crystallizing system are housed on connecting line
The crystal output end connection salt of system melts crystal system, and the mother liquor output end of freezing and crystallizing system connects organic upgrading unit, organic
The concentrated water output end of upgrading unit connects the second oxidation reactor, and the output end of the second oxidation reactor connects back to intermediate pool,
The production water output end of organic upgrading unit connects the second drier, and the output end connection carnallite collection bag of the second drier, salt melts
The output end of crystal system connects the 3rd drier, the output end connection sodium sulphate Product recycling bag of the 3rd drier.
Beneficial effect
The special equipment of the separation of salt and crystallization process for reclaiming, passes through first in the brine waste that the utility model is provided
Nanofiltration separates the sodium chloride in brine waste and sodium sulphate, nanofiltration produce water by oxidation, evaporative crystallization, be dried to obtain chlorine
Change sodium product, nanofiltration concentrated water first passes through freezing and crystallizing and obtains sal glauberi crystal, then melting large particle crystal by salt again will
Sal glauberi crystal transformation is large grain anhydrous sodium sulfate product, it is to avoid product salt granularity in single refrigeration crystallization process
Carefully, the problem of difficult caking is dehydrated, carnallite yield is reduced, reduces pollution, save a large amount of carnallites as fixed-end forces
Cost, and two kinds of sodium salt recyclings, can create economic value.
Brief description of the drawings
Accompanying drawing 1 is the process chart of the utility model embodiment.
Accompanying drawing 2 is the equipment connecting relation schematic diagram of the utility model embodiment.
Embodiment
With reference to the accompanying drawings and examples, the utility model is described further.
Embodiment
As shown in Figure 2, in brine waste salt separation and crystallize process for reclaiming special equipment, it include pretreatment
Reactor 3, nano-filtration unit 4, the first oxidation reactor 5, evaporation and crystallization system 6, the second oxidation reactor 9, freezing and crystallizing system
12nd, organic upgrading unit 13 and salt melt crystal system 16；
Former pond 1 is connected with preatreating reactors 3, and the first intake pump 2 is housed on connecting line, preatreating reactors 3
Output end connects nano-filtration unit 4, and the production water output end of nano-filtration unit 4 connects the first oxidation reactor 5, the concentrated water of nano-filtration unit 4
Output end connects intermediate pool 10, and the output end of the first oxidation reactor 5 connects evaporation and crystallization system 6, evaporation and crystallization system 6
Crystal output end connects the first drier 7, and the mother liquor output end of evaporation and crystallization system 6 connects the second drier 14, and first dries
The output end connection sodium chloride Product recycling bag 8 of device 7, intermediate pool 10 is connected with freezing and crystallizing system 12, is filled on connecting line
There is the second intake pump 11, the crystal output end connection salt of freezing and crystallizing system 12 melts crystal system 16, freezing and crystallizing system 12
Mother liquor output end connects organic upgrading unit 13, and the concentrated water output end of organic upgrading unit 13 connects the second oxidation reactor 9, the
The output end of titanium dioxide reactor 9 connects back to intermediate pool 10, and the production water output end connection second of organic upgrading unit 13 is dried
Device 14, the output end connection carnallite collection bag 15 of the second drier 14, the output end connection the 3rd that salt melts crystal system 16 is dried
Device 17, the output end connection sodium sulphate Product recycling bag 18 of the 3rd drier 17.
As shown in Figure 1, separation and the crystallization process for reclaiming mistake of salt in brine waste are carried out using above-mentioned special equipment
Journey is as follows：
The first step：Brine waste (is mainly contained into Cl-, SO4 2-、Na+, and a small amount of organic matter, K+、NO3- etc.) be pumped into
In pretreatment system, preprocessing process, alkali is firstly added, calcium, magnesium plasma in waste water is removed, then adds a small amount of strong acid, is adjusted
The pH value of waste water is saved between 5~7, the separation in favor of subsequent nano-filtration film to organic matter and salt finally gives pretreatment water outlet.
Second step：The pretreatment water outlet of the first step enters nanofiltration system, is carried out under (10~30) bar operating pressure dense
Division is from containing chlorion and small organic molecule through film formation production water, sulfate ion and larger molecular organicses are trapped
Form concentrated water.Organic matter and divalent ion of the main molecular cut off of the NF membrane between 200~400.
3rd step：The nanofiltration production water of second step is introduced into oxidative system, is firstly added strong oxidizer, oxidation Decomposition is removed and received
Small organic molecule (being beneficial to the sodium chloride salt for subsequently obtaining high-purity) in filter production water, is then evaporated crystallization, obtains again
Sodium chloride crystal and mother liquor, crystal obtain sodium chloride product after drying.
Meanwhile, the nanofiltration concentrated water of second step enters freezing and crystallizing system, and now the concentrated water is reduced rapidly to 0 DEG C or so, knot
Crystalline substance obtains sal glauberi crystal, and then the crystal enters salt and melts large particle crystal system, and temperature is risen to after (35~50) DEG C,
The crystallization water is lost, large grain anhydrous sodium sulfate is obtained, eventually passes and obtains sodium sulphate product after drying.Wherein, freezing and crystallizing mistake
A certain amount of mother liquor is produced in journey, mother liquor enters organic concentrate system.
4th step：The freezing and crystallizing mother liquor of 3rd step is entered into organic concentration systems, in (15~40) bar operating pressures
Under, by the retention centrifugation of film, the larger molecular organicses in freezing and crystallizing mother liquor and part small organic molecule are carried out
Retention forms concentrated water, and the small organic molecule of salt and another part is through film formation production water.Wherein, the steaming of production water and the 3rd step
Hair crystalline mother solution enters drying system simultaneously, and carnallite is obtained after drying.
5th step：Organic concentration production water of 4th step is entered into oxidative system, strong oxidizer is firstly added, small molecule is had
The oxidation production water that machine thing oxidative degradation (avoiding small organic molecule from being accumulated in system) is obtained returns to freezing and crystallizing system circulation
Reprocessing, can carry out crystallization precipitation again by sodium sulphate remaining in water.
Claims (1)
1. the special equipment of the separation of salt and crystallization process for reclaiming in brine waste, it is characterised in that：It is anti-that it includes pretreatment
Answer device (3), nano-filtration unit (4), the first oxidation reactor (5), evaporation and crystallization system (6), the second oxidation reactor (9), freezing
Crystal system (12), organic upgrading unit (13) and salt melt crystal system (16)；
Former pond (1) is connected with preatreating reactors (3), and the first intake pump (2), preatreating reactors are housed on connecting line
(3) output end connection nano-filtration unit (4), the production water output end of nano-filtration unit (4) connects the first oxidation reactor (5), nanofiltration
The concentrated water output end connection intermediate pool (10) of unit (4), the output end connection evaporation and crystallization system of the first oxidation reactor (5)
(6), the crystal output end of evaporation and crystallization system (6) connects the first drier (7), the mother liquor output end of evaporation and crystallization system (6)
Connect the second drier (14), the output end connection sodium chloride Product recycling bag (8) of the first drier (7), intermediate pool (10)
It is connected with freezing and crystallizing system (12), the second intake pump (11) is housed on connecting line, the crystal of freezing and crystallizing system (12) is defeated
Go out end connection salt and melt crystal system (16), the mother liquor output end of freezing and crystallizing system (12) connects organic upgrading unit (13), had
The concentrated water output end of machine upgrading unit (13) connects the second oxidation reactor (9), the output end connection of the second oxidation reactor (9)
Intermediate pool (10) is returned, the production water output end of organic upgrading unit (13) connects the second drier (14), the second drier (14)
Output end connection carnallite collection bag (15), salt melt crystal system (16) output end connection the 3rd drier (17), the 3rd is dry
The output end connection sodium sulphate Product recycling bag (18) of dry device (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621406066.1U CN206359377U (en) | 2016-12-21 | 2016-12-21 | The special equipment of the separation of salt and crystallization process for reclaiming in brine waste |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621406066.1U CN206359377U (en) | 2016-12-21 | 2016-12-21 | The special equipment of the separation of salt and crystallization process for reclaiming in brine waste |
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| CN206359377U true CN206359377U (en) | 2017-07-28 |
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| CN109422314A (en) * | 2017-08-28 | 2019-03-05 | 中国石油化工股份有限公司 | The processing method of catalyst production waste water |
| CN109422406A (en) * | 2017-08-28 | 2019-03-05 | 中国石油化工股份有限公司 | The processing method of catalyst production waste water |
| CN109422403A (en) * | 2017-08-28 | 2019-03-05 | 中国石油化工股份有限公司 | The processing method of catalyst production waste water |
| CN109422399A (en) * | 2017-08-28 | 2019-03-05 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN110451706A (en) * | 2019-05-13 | 2019-11-15 | 上海晶宇环境工程股份有限公司 | The separating technology and special equipment of high-enriched organics and salt during strong brine zero-emission |
| CN113912231A (en) * | 2021-07-13 | 2022-01-11 | 北京航天环境工程有限公司 | System and method for recycling and co-processing wastewater |
| CN109422396B (en) * | 2017-08-28 | 2023-02-24 | 中国石油化工股份有限公司 | Method for treating wastewater from catalyst production |
| CN109422394B (en) * | 2017-08-28 | 2023-04-07 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN109422397B (en) * | 2017-08-28 | 2023-04-07 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| US11820690B2 (en) | 2017-08-28 | 2023-11-21 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
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| CN109422397B (en) * | 2017-08-28 | 2023-04-07 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN109422399B (en) * | 2017-08-28 | 2023-02-17 | 中国石油化工股份有限公司 | Method for treating waste water containing ammonium salt |
| CN109422403A (en) * | 2017-08-28 | 2019-03-05 | 中国石油化工股份有限公司 | The processing method of catalyst production waste water |
| CN109422399A (en) * | 2017-08-28 | 2019-03-05 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN109422396B (en) * | 2017-08-28 | 2023-02-24 | 中国石油化工股份有限公司 | Method for treating wastewater from catalyst production |
| US11820690B2 (en) | 2017-08-28 | 2023-11-21 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
| CN109422406A (en) * | 2017-08-28 | 2019-03-05 | 中国石油化工股份有限公司 | The processing method of catalyst production waste water |
| CN109422403B (en) * | 2017-08-28 | 2023-02-24 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN109422314A (en) * | 2017-08-28 | 2019-03-05 | 中国石油化工股份有限公司 | The processing method of catalyst production waste water |
| CN109422314B (en) * | 2017-08-28 | 2023-03-28 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN109422406B (en) * | 2017-08-28 | 2023-04-07 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN109422394B (en) * | 2017-08-28 | 2023-04-07 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN110451706A (en) * | 2019-05-13 | 2019-11-15 | 上海晶宇环境工程股份有限公司 | The separating technology and special equipment of high-enriched organics and salt during strong brine zero-emission |
| CN110451706B (en) * | 2019-05-13 | 2023-10-27 | 上海晶宇环境工程股份有限公司 | Separation process of high-concentration organic matters and salt in zero-emission process of strong brine and special equipment |
| CN113912231B (en) * | 2021-07-13 | 2023-09-26 | 北京航天环境工程有限公司 | System and method for resource co-processing of wastewater |
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