CN103058303B - Method for separating inorganic salt substances from high-salt liquid waste - Google Patents
Method for separating inorganic salt substances from high-salt liquid waste Download PDFInfo
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- CN103058303B CN103058303B CN2012104894019A CN201210489401A CN103058303B CN 103058303 B CN103058303 B CN 103058303B CN 2012104894019 A CN2012104894019 A CN 2012104894019A CN 201210489401 A CN201210489401 A CN 201210489401A CN 103058303 B CN103058303 B CN 103058303B
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- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000010808 liquid waste Substances 0.000 title claims abstract description 26
- 229910017053 inorganic salt Inorganic materials 0.000 title claims abstract description 12
- 239000000126 substance Substances 0.000 title abstract description 5
- 150000003839 salts Chemical class 0.000 claims abstract description 48
- 239000006200 vaporizer Substances 0.000 claims abstract description 45
- 238000001816 cooling Methods 0.000 claims abstract description 23
- 239000002002 slurry Substances 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 18
- 238000001704 evaporation Methods 0.000 claims abstract description 15
- 230000008020 evaporation Effects 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 239000002351 wastewater Substances 0.000 claims description 21
- 239000010409 thin film Substances 0.000 claims description 20
- 230000008569 process Effects 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 239000012141 concentrate Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000004065 wastewater treatment Methods 0.000 abstract description 5
- 239000000203 mixture Substances 0.000 abstract description 4
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 238000009834 vaporization Methods 0.000 abstract 3
- 230000008016 vaporization Effects 0.000 abstract 3
- 238000007599 discharging Methods 0.000 abstract 2
- 239000000243 solution Substances 0.000 description 23
- 238000005516 engineering process Methods 0.000 description 4
- 235000019600 saltiness Nutrition 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000003905 agrochemical Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 239000000975 dye Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 229910001069 Ti alloy Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 239000007770 graphite material Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000009938 salting Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
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- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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Abstract
The invention discloses a method for separating inorganic salt substances from high-salt liquid waste, belonging to wastewater treatment of the environment protection field. A system sequentially comprises an evaporator, a vaporizer, a film evaporator and a cooling spiral pusher. The method comprises the following steps of: conveying the high-salt liquid waste into the evaporator from the lower end of the evaporator by a pump, heating the high-salt liquid waste, conveying the high-salt liquid waste through a pipeline into the vaporizer for vaporization and flash separation; discharging the steam from the upper end outlet of the vaporizer, and condensing the steam; obtaining concentrated solution of the high-salt liquid waste in the vaporizer after executing vaporization and flash separation; discharging the concentrated solution from the circulating discharge port at the lower end of the vaporizer through a pipe and conveying the concentrated solution into the evaporator again from the feed port at the lower end of the evaporator, mixing the concentrated solution with the high-salt liquid waste, heating the mixture again, and executing vaporization and evaporation to further get the concentrated solution, and conveying the concentrated solution into the film evaporator from the lower end of the vaporizer through the pipe to obtain the salt slurry; and conveying the salt slurry into the cooling spiral pusher to get the salty mud, thereby realizing effective separation from the inorganic salt substances. The method is high in efficiency and low in energy consumption.
Description
Technical field
The present invention relates to the separating treatment of inorganic salt in high salt bearing liquid wastes, belong to the field of environment protection of wastewater treatment.
Background technology
High salt bearing liquid wastes refer to contain organism and at least the massfraction of total dissolved solidss TDS be greater than the i.e. waste water more than 6% of twice concentration of seawater.Usually in this class waste water except containing a large amount of inorganic salt, as Cl
-, Na
+, SO
4 2-, Ca
2+Deng outside, also contain organic pollutant.Be mainly derived from: (1) Chemical Manufacture: chemical reaction not exclusively or the chemical reaction by product, especially produces the toxic wastewater of a large amount of high COD, high salt in the Chemicals such as agricultural chemicals, dyestuff production process.(2) wastewater treatment, cycling and reutilization produce.In wastewater treatment process, the own saltiness of the waste water brought that adds of water conditioner and acid, alkali increases; Waste water is through processing, the more highly enriched liquid of salinity produced in COD water cycle recycling up to standard process.All these is referred to as high saltness waste liquid.The high salt bearing liquid wastes of this class, not only more common sewage has larger contaminative, and can be to the soil salinization, form saltings, thereby the vegetation of spoiled soil.
For the high saliferous produced in the chemical processs such as agricultural chemicals, dyestuff, high-COD waste water, usually adopt the method for directly burning to be processed.This method is waste water to be to vaporific spray in high temperature combustion furnace, and water smoke is vaporized fully, allows organism oxidation in stove in waste water, is decomposed into perfect combustion product carbonic acid gas and water and inorganic salt ash content.It is generally acknowledged that the high salt bearing liquid wastes of COD >=100000mg/L, calorific value >=2500kcal/kg or the salty organic waste liquid of organic composition massfraction >=10% adopt burning method to process than additive method more economically, rationally.Obviously, it is very uneconomic taking the method for directly burning for other high slat-containing wastewater.After all, burn power consumption high, easily produce flue gas and cause the pollution to atmosphere.
Usually adopt the principle of evaporation to carry out evaporation concentration to high slat-containing wastewater, obtain high saliferous concentrating spent liquor.Finally, take degree of depth cooling technology, by cooling and crystallizing process, make inorganic salt wherein obtain separating treatment.Simultaneously, be recycled still very high concentrated solution of water and saltiness.Wherein, concentrated solution returns to the leading portion operation and is evaporated, concentrates, and crystallisation by cooling, realize the further separation of inorganic salts material.Yet, because the salt in waste water is mostly the muriate of solubility, solubleness is very large and temperature influence is less.Therefore, the separation efficiency that adopts the crystallisation by cooling technology to carry out the inorganic salts material to concentrated salt bearing liquid wastes is very low.Particularly, crystalline mother solution returns to FEOL and is reheated evaporation.Cause that whole technical process is long, energy consumption is high.Thus, in the urgent need to developing the separation method of inorganic salt material in a kind of efficient, high salt bearing liquid wastes that energy consumption is lower.
Summary of the invention
The present invention seeks to develop the separation method of inorganic salt material in a kind of efficient, high salt bearing liquid wastes that energy consumption is lower.
The method for separating and processing of inorganic salt material in a kind of high salt bearing liquid wastes is characterized in that:
The system of application comprises following equipment successively: vaporizer, vaporizer, thin-film evaporator, cooling spiral pushing device;
Using pump that high salt bearing liquid wastes is sent into and heated from the vaporizer lower end, control 105～120 ℃ of evaporator outlet temperatures. heated high salt bearing liquid wastes enters vaporizer from the vaporizer upper end by pipeline, is vaporized, flash separation; Wherein, 60～70% water becomes water vapour, and is exported out by the vaporizer upper end and enter condenser and carry out condensation, becomes recycle-water;
Enter the high salt bearing liquid wastes in vaporizer, after overflash, flash separation, remaining 30～40% concentrated liquid; Concentrated liquid enters from the opening for feed of vaporizer lower end from vaporizer lower end circulation discharge port again by pipeline, mixes again with high slat-containing wastewater and heats, vaporizes, evaporates, and further concentrates and obtains concentrated solution, makes the proportion of concentrated solution reach 1.4～1.6;
This concentrated solution enters the thin-film evaporator upper end by pipeline from the vaporizer lower end, carries out thin film evaporation, makes the water evaporation 70～80% in concentrated solution, and the steam temperature out is controlled at 100～110 ℃, the salt slurry of remaining 20-30%; This salt slurry enters the cooling spiral pushing device, cooling by obtaining in the helical feed process, makes its temperature be reduced to 30～40 ℃. and last, by the cooling spiral pushing device, discharged, obtain salt slurry, thereby realize effective separation of inorganic salts material;
In whole technical process, all adopt induced draft fan to maintain operation under the micro-vacuum state of system in 85～95kpa, operation.
Key equipment and process control parameter
1. thin-film evaporator
(1) material of thin-film evaporator is the 316L stainless steel, and titanium alloy or corrosion-resistant high-temperature graphite material process.It belongs to vertical equipment, adopts steam heating.The aspect ratio of thin-film evaporator is greater than 2, on the end socket of upper end, arranges by concentrated solution opening for feed, steam outlet and clear water rinse mouth, and the lower end end socket is arranged by salt slurry discharge port.The turning axle of inner mounting strap scraper plate, and on the top of turning axle, the seal pot by concentrated solution is installed.At first concentrated solution enters seal pot by upper end end socket opening for feed.Seal pot is along with turning axle rotates together, and its speed of rotation is controlled at 45～60 rev/mins.Concentrated solution is fallen to the inwall that is sprinkled upon thin-film evaporator, and heated and evaporate.In this process, concentrated solution, along with evaporation of water, becomes the salt slurry gradually, and discharge the bottom of the scraper plate effect current downflow thin-film evaporator on turning axle.Wherein, water vapour is discharged by the steam outlet of baudelot evaporator upper end.During this time, control 100～110 ℃ of steam temperature outs.
(2) critical process is controlled parameter
1) temperature out of vaporizer is controlled at 105～120 ℃; The steam output that concentrated solution enters in vaporizer is 60～70%;
2) the salt slurry carries out thin film evaporation in thin-film evaporator, and the steam temperature out is controlled at 100～110 ℃, the water evaporation 70-80% in the salt slurry;
3) the vaporizer lower end enters the specific gravity control of concentrated solution of thin-film evaporator 1.4～1.6;
4) adopt induced draft fan to maintain system operates, moves under micro-vacuum state.
The present invention utilizes thin film evaporation equipment, adopts single flash-thin film evaporation-salt slurry process for cooling technology, realizes the method for separating and processing of inorganic salts material in high salt bearing liquid wastes.The method efficiency is high, energy consumption is lower.
Embodiment
Example 1
The high slat-containing wastewater that a kind of pesticide producing produces, its saltiness 10～15%, COD is 300～500mg/L.This waste water is used pump to send into and heated from the vaporizer lower end, controls 115 ℃ of evaporator outlet temperatures. and heated high slat-containing wastewater enters vaporizer from the vaporizer upper end by pipeline, is vaporized, flash separation.Wherein, 70% water becomes water vapour, and is exported out by the vaporizer upper end and enter condenser and carry out condensation, becomes recycle-water.
Enter the high salt bearing liquid wastes in vaporizer, after overflash, flash separation, remaining 30% concentrated solution.Concentrated solution enters from the opening for feed of vaporizer lower end from vaporizer lower end circulation discharge port again by pipeline, mix again with high slat-containing wastewater and heat, vaporize, evaporate, further concentrated, make the proportion of its concentrated solution reach 1.3, again this concentrated solution is entered to the thin-film evaporator upper end by pipeline from the vaporizer lower end, again carry out thin film evaporation, the steam temperature out is controlled at 100 ℃, make the water in its concentrated solution evaporate again 80%, remaining 20% salt slurry.This salt slurry enters the cooling spiral pushing device, cooling by obtaining in the helical feed process, makes its temperature be reduced to 30 ℃. and last, by the cooling spiral pushing device, discharged, obtain salt slurry.
Salt slurry, under the effect of cooling spiral pushing device, is sent into salt slurry to be burned from the rotary incinerator upper end.Incineration temperature is controlled 450 ℃, stops 3 minutes burning time.Finally, high-temp solid salt slag, under the turning effort of rotary incinerator, is discharged from its lower end.In burning process, by the high-temperature flue gas discharge after washing, cooling, purification produced.
In whole technical process, all adopt induced draft fan to maintain system and operate under micro-vacuum state, move.
Example 2
Certain waste water treatment plant's waste water is through processing, and COD is less than 100mg/L.In order to realize " zero " discharge, this qualified discharge water realizes adopting reverse osmosis membrane to be processed, and reclaims 80% water circulation use.20% remaining density wastewater during passes through multi-effect flashing steam again, by its evaporation, reclaims 80% water.20% remaining dense waste liquid.This waste water utilization pump is sent into and is heated from the vaporizer lower end, controls 105 ℃ of evaporator outlet temperatures. and heated dense waste liquid enters vaporizer from the vaporizer upper end by pipeline, is vaporized, flash separation.Wherein, 60% water becomes water vapour, and is exported out by the vaporizer upper end and enter condenser and carry out condensation, becomes recycle-water.
Enter the high salt bearing liquid wastes in vaporizer, after overflash, flash separation, remaining 40% concentrated solution.Concentrated solution enters from the opening for feed of vaporizer lower end from vaporizer lower end circulation discharge port again by pipeline, mix again with high slat-containing wastewater and heat, vaporize, evaporate, further concentrated, make the proportion of its concentrated solution reach 1.3, again this concentrated solution is entered to the thin-film evaporator upper end by pipeline from the vaporizer lower end, carry out thin film evaporation, the steam temperature out is controlled at 110 ℃, make the water in its concentrated solution evaporate again 70%, remaining 30% salt slurry.This salt slurry enters the cooling spiral pushing device, cooling by obtaining in the helical feed process, makes its temperature be reduced to 30 ℃. and last, by the cooling spiral pushing device, discharged, obtain salt slurry, realize effective separation of inorganic salts material.
Claims (1)
1. the method for separating and processing of inorganic salt material in a high salt bearing liquid wastes is characterized in that:
The system of application comprises following equipment successively: vaporizer, vaporizer, thin-film evaporator, cooling spiral pushing device;
Use pump that high salt bearing liquid wastes is sent into and heated from the vaporizer lower end, control 105～120 ℃ of evaporator outlet temperatures; Heated high salt bearing liquid wastes enters vaporizer from the vaporizer upper end by pipeline, is vaporized, flash separation; Wherein, 60～70% water becomes water vapour, and is exported out by the vaporizer upper end and enter condenser and carry out condensation, becomes recycle-water;
Enter the high salt bearing liquid wastes in vaporizer, after overflash, flash separation, remaining 30～40% concentrated liquid; Concentrated liquid enters from the opening for feed of vaporizer lower end from vaporizer lower end circulation discharge port again by pipeline, mixes again with high slat-containing wastewater and heats, vaporizes, evaporates, and further concentrates and obtains concentrated solution, makes the proportion of concentrated solution reach 1.4～1.6;
This concentrated solution enters the thin-film evaporator upper end by pipeline from the vaporizer lower end, carries out thin film evaporation, makes the water evaporation 70～80% in concentrated solution, and the steam temperature out is controlled at 100～110 ℃, the salt slurry of remaining 20-30%; This salt slurry enters the cooling spiral pushing device, cooling by obtaining in the helical feed process, makes its temperature be reduced to 30～40 ℃; Finally, by the cooling spiral pushing device, discharged, obtain salt slurry, thereby realize effective separation of inorganic salts material;
In whole technical process, all adopt induced draft fan to maintain operation under the micro-vacuum state of system in 85～95kpa, operation.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012104894019A CN103058303B (en) | 2012-11-26 | 2012-11-26 | Method for separating inorganic salt substances from high-salt liquid waste |
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| CN107324431B (en) * | 2017-08-10 | 2023-05-23 | 江苏省环境科学研究院 | Segmented gasification detoxification system and method for high-concentration organic salt-containing waste liquid |
| CN111003866B (en) * | 2019-12-06 | 2024-05-17 | 安徽晨晰洁净科技有限公司 | Waste salt concentration treatment device |
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| SE366282B (en) * | 1972-08-28 | 1974-04-22 | Atomenergi Ab | |
| DE2531295A1 (en) * | 1975-07-12 | 1977-01-20 | Naman Azhari | DISTILLATION PLANT COMBINED WITH A STEAM POWER PLANT FOR DESALINATION OF SEA WATER |
| CN202063789U (en) * | 2011-05-06 | 2011-12-07 | 山东光大科技发展有限公司 | Treatment device for waste water containing salt |
| CN102433212B (en) * | 2011-10-19 | 2016-08-03 | 北京生态岛科技有限责任公司 | The method of purification of waste lubricating oil and device |
| CN102701303B (en) * | 2012-05-29 | 2013-11-13 | 汪亮亮 | Liquid-film low-temperature-evaporation zero-emission saline wastewater treatment method |
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