CN103058303A - 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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- CN103058303A CN103058303A CN2012104894019A CN201210489401A CN103058303A CN 103058303 A CN103058303 A CN 103058303A CN 2012104894019 A CN2012104894019 A CN 2012104894019A CN 201210489401 A CN201210489401 A CN 201210489401A CN 103058303 A CN103058303 A CN 103058303A
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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 the 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 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, such 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, the dyestuff production process.(2) wastewater treatment, cycling and reutilization produce.In wastewater treatment process, the saltiness of the waste water that the adding of water conditioner and acid, alkali brings own increases; Waste water is through processing the more highly enriched liquid of salinity that produces in the 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 the saltings, thereby the vegetation of spoiled soil.
Usually adopt the method for directly burning to process for the high saliferous that produces in the chemical processs such as agricultural chemicals, dyestuff, high-COD waste water.This method is waste water to be vaporific spray in the high temperature combustion furnace, and water smoke is vaporized fully, allows organism oxidation in stove in the 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, the method for taking directly to burn for other high slat-containing wastewater is very uneconomic.After all, burn power consumption high, easily produce flue gas and cause pollution to atmosphere.
Usually adopt the principle of evaporation that high slat-containing wastewater is carried out evaporation concentration, obtain high saliferous concentrating spent liquor.At last, 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 the leading portion operation and evaporates, concentrates, and crystallisation by cooling is realized the further separation of inorganic salts material.Yet because the salt in the waste water mostly is the muriate of solubility, solubleness is very large and temperature influence is less.Therefore, adopt the crystallisation by cooling technology very low to the separation efficiency that concentrated salt bearing liquid wastes carries out the inorganic salts material.Particularly, crystalline mother solution returns FEOL and reheats 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 that uses comprises following equipment successively: vaporizer, vaporizer, thin-film evaporator, cooling spiral pushing device;
Using pump that high salt bearing liquid wastes is sent into from the vaporizer lower end and heat, 105 ~ 120 ℃ of control evaporator outlet temperatures. heated high salt bearing liquid wastes enters vaporizer from the vaporizer upper end by pipeline, vaporizes, flash separation; Wherein, 60 ~ 70% water becomes water vapour, and is exported out by vaporizer upper end and enter condenser and carry out condensation, becomes recycle-water;
Enter the high salt bearing liquid wastes in the 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 ~ 1.6g;
This concentrated solution enters the thin-film evaporator upper end by pipeline from the vaporizer lower end, carry out thin film evaporation, makes the water evaporation 70 ~ 80% in the 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, by being cooled off in the helical feed process, makes its temperature be reduced to 30 ~ 40 ℃. and last, discharged by the cooling spiral pushing device, obtain salt slurry, thereby realize the effective separation of inorganic salts material;
In whole technical process, all adopt induced draft fan to keep operation under the micro-vacuum state that system is 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 arranges on the end socket of upper end that greater than 2 by concentrated solution opening for feed, steam outlet and flushing with clean water mouth, the lower end end socket is arranged by salt and starched discharge port.The turning axle of inner mounting strap scraper plate, and at the seal pot of the top of turning axle installation by concentrated solution.Concentrated solution at first 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 the inwall that is sprinkled upon thin-film evaporator, and heated and evaporate.In this process, concentrated solution becomes the salt slurry gradually along with evaporation of water, and discharge the bottom of the scraper plate effect current downflow thin-film evaporator on turning axle.Wherein, water vapour is then discharged by the steam outlet of baudelot evaporator upper end.During this time, control steam temperature out is 100 ~ 110 ℃.
(2) critical process control parameter
1) temperature out of vaporizer is controlled at 105 ~ 120 ℃. and the steam output that concentrated solution enters in the 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 ℃, and steam output is 70-~ 80%;
3) the vaporizer lower end enters the specific gravity control of concentrated solution of thin-film evaporator at 1.4 ~ 1.6g;
4) adopt induced draft fan to keep system and be in operation under the micro-vacuum state, operation.
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 the high salt bearing liquid wastes.The method efficient is high, energy consumption is lower.
Description of drawings
Fig. 1 is apparatus of the present invention schematic diagram.
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 uses pump to send into from the vaporizer lower end to heat 115 ℃ of control evaporator outlet temperatures. and heated high slat-containing wastewater enters vaporizer from the vaporizer upper end by pipeline, vaporizes, flash separation.Wherein, 70% water becomes water vapour, and is exported out by vaporizer upper end and enter condenser and carry out condensation, becomes recycle-water.
Enter the high salt bearing liquid wastes in the 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 to heat, vaporize, to evaporate, further concentrated, make the proportion of its concentrated solution reach 1.3g. and again this concentrated solution is entered 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 ℃, makes the water revaporization 80% in its concentrated solution, remaining 20% salt slurry.This salt slurry enters the cooling spiral pushing device, by being cooled off in the helical feed process, makes its temperature be reduced to 30 ℃. and last, discharged by the cooling spiral pushing device, obtain salt slurry.
Salt slurry is sent into salt slurry and to be burned under the effect of cooling spiral pushing device from rotary incinerator upper end.450 ℃ of incineration temperature controls stop 3 minutes burning time.At last, high-temp solid salt slag is discharged from its lower end under the turning effort of rotary incinerator.In burning process, with the high-temperature flue gas that produces through washing, cooling, purify after discharging.
In whole technical process, all adopt induced draft fan to keep system and be in operation under the micro-vacuum state, operation.
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 " discharging, this qualified discharge water realizes adopting reverse osmosis membrane to process, and reclaims 80% water circulation use.20% remaining density wastewater during passes through multi-effect flashing steam again, with its evaporation, reclaims 80% water.20% remaining dense waste liquid.This waste water utilization pump is sent into from the vaporizer lower end and is heated, 105 ℃ of evaporator outlet temperatures of control. and heated dense waste liquid enters vaporizer from the vaporizer upper end by pipeline, vaporizes, flash separation.Wherein, 60% water becomes water vapour, and is exported out by vaporizer upper end and enter condenser and carry out condensation, becomes recycle-water.
Enter the high salt bearing liquid wastes in the 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 to heat, vaporize, to evaporate, further concentrated, make the proportion of its concentrated solution reach 1.3g. and again this concentrated solution is entered 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 ℃, makes the water revaporization 70% in its concentrated solution, remaining 30% salt slurry.This salt slurry enters the cooling spiral pushing device, by being cooled off in the helical feed process, makes its temperature be reduced to 30 ℃. and last, discharged by the cooling spiral pushing device, obtain salt slurry, realize the effective separation of inorganic salts material.
Claims (1)
1. the method for separating and processing of inorganic salt material in the high salt bearing liquid wastes is characterized in that:
The system that uses comprises following equipment successively: vaporizer, vaporizer, thin-film evaporator, cooling spiral pushing device;
Using pump that high salt bearing liquid wastes is sent into from the vaporizer lower end and heat, 105 ~ 120 ℃ of control evaporator outlet temperatures. heated high salt bearing liquid wastes enters vaporizer from the vaporizer upper end by pipeline, vaporizes, flash separation; Wherein, 60 ~ 70% water becomes water vapour, and is exported out by vaporizer upper end and enter condenser and carry out condensation, becomes recycle-water;
Enter the high salt bearing liquid wastes in the 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 ~ 1.6g;
This concentrated solution enters the thin-film evaporator upper end by pipeline from the vaporizer lower end, carry out thin film evaporation, makes the water evaporation 70 ~ 80% in the 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, by being cooled off in the helical feed process, makes its temperature be reduced to 30 ~ 40 ℃. and last, discharged by the cooling spiral pushing device, obtain salt slurry, thereby realize the effective separation of inorganic salts material;
In whole technical process, all adopt induced draft fan to keep operation under the micro-vacuum state that system is in 85 ~ 95Kpa, operation.
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| CN2012104894019A CN103058303B (en) | 2012-11-26 | 2012-11-26 | Method for separating inorganic salt substances from high-salt liquid waste |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107324431A (en) * | 2017-08-10 | 2017-11-07 | 江苏省环境科学研究院 | A kind of organic salt bearing liquid wastes segmented gasification detoxification system and method for high concentration |
| CN111003866A (en) * | 2019-12-06 | 2020-04-14 | 安徽晨晰洁净科技有限公司 | Waste salt concentration treatment device |
| 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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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107324431A (en) * | 2017-08-10 | 2017-11-07 | 江苏省环境科学研究院 | A kind of organic salt bearing liquid wastes segmented gasification detoxification system and method for high concentration |
| 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 |
| CN111003866A (en) * | 2019-12-06 | 2020-04-14 | 安徽晨晰洁净科技有限公司 | Waste salt concentration treatment device |
| 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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