CN111494974A - High-salinity wastewater reduction treatment method applied to thermal power plant - Google Patents
High-salinity wastewater reduction treatment method applied to thermal power plant Download PDFInfo
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- CN111494974A CN111494974A CN202010222584.2A CN202010222584A CN111494974A CN 111494974 A CN111494974 A CN 111494974A CN 202010222584 A CN202010222584 A CN 202010222584A CN 111494974 A CN111494974 A CN 111494974A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0082—Regulation; Control
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0094—Evaporating with forced circulation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/06—Evaporators with vertical tubes
- B01D1/065—Evaporators with vertical tubes by film evaporating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
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- Environmental & Geological Engineering (AREA)
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- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a high-salt-content wastewater reduction treatment method applied to a thermal power plant, which is applied to a wastewater treatment system, and comprises the following steps: seed crystal adding step: adding a proper amount of seed crystals to the vertical falling film evaporator; preheating: the stock solution is sent to a preheater for preheating, and then the preheated stock solution is sent to a vertical falling-film evaporator; and (3) an evaporation step: circularly evaporating and concentrating the stock solution in a vertical falling-film evaporator; and (3) grain recovery: and (3) conveying the concentrated solution to a hydrocyclone, separating the seed crystals by the hydrocyclone, sending the separated seed crystals back to the vertical falling-film evaporator, and sending the concentrated solution from which the seed crystals are separated to a concentrated solution tank. In the process of evaporation concentration, although the waste water is continuously concentrated and reduced, the seed crystal balance in the circulating liquid (in the bottom liquid cavity) is effectively maintained, and the inner wall of the bottom liquid cavity is not easy to scale, so that the working performance of the evaporator is maintained.
Description
Technical Field
The invention relates to a wastewater treatment method, in particular to a reduction treatment method for high-salt-content wastewater of a thermal power plant.
Background
The waste water of the thermal power plant comprises domestic sewage and industrial waste water, the quality of various waste water is different, the treatment scale is large, the difficulty is high, and the energy consumption is large. With the national requirements on wastewater discharge standards becoming stricter, the "wastewater reduction" and "wastewater zero discharge" will become the trend of non-blocking, and how to effectively treat and recycle wastewater is a problem generally faced by current thermal power plants. At present, most of domestic wastewater treatment systems of thermal power plants can only treat general industrial wastewater and domestic sewage, and have poor treatment effects on high-salt wastewater such as chemical acid-base regenerated high-salt wastewater, fine-treatment regenerated high-salt wastewater, desulfurization wastewater and the like. At present, the membrane concentration technology and the thermal method concentration technology are mostly applied to wastewater reduction. However, the membrane concentration feed water has strict requirements, and the process operation requirements of membrane concentration can be met only by carrying out strict pretreatment, so that the investment and the operation cost are increased. The thermal method concentration utilizes a heat source to heat the wastewater technology so as to continuously evaporate water molecules, thereby continuously concentrating and reducing the wastewater. At present, a plurality of multi-effect evaporation technologies and vapor mechanical recompression evaporation technologies are used, the energy consumption in the evaporation process is high, equipment is easy to scale, and the performance of the equipment is seriously influenced. Therefore, the treatment of high-salinity wastewater from thermal power plants remains to be improved.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide a reduction treatment method for high-salt-content wastewater of a thermal power plant, which can avoid easy scaling, thereby ensuring the performance of equipment.
The purpose of the invention is realized by adopting the following technical scheme:
a reduction treatment method for high-salt-content wastewater of a thermal power plant is applied to a wastewater treatment system, and comprises the following steps:
seed crystal adding step: adding a proper amount of seed crystals to the vertical falling film evaporator;
preheating: the stock solution is sent to a preheater for preheating, and then the preheated stock solution is sent to a vertical falling-film evaporator;
and (3) an evaporation step: circularly evaporating and concentrating the stock solution in a vertical falling-film evaporator;
and (3) grain recovery: and (3) conveying the concentrated solution to a hydrocyclone, separating the seed crystals by the hydrocyclone, sending the separated seed crystals back to the vertical falling-film evaporator, and sending the concentrated solution from which the seed crystals are separated to a concentrated solution tank.
Specifically, in the preheating step, the stock solution is preheated to 55-65 ℃.
Specifically, in the evaporation step, the evaporation temperature of the vertical falling-film evaporator is 90-100 ℃.
Specifically, the method comprises a steam pressurizing step, wherein the steam pressurizing step comprises the following steps:
saturated steam generated by the work of the vertical falling-film evaporator is sent to a steam compressor, the steam compressor applies work to the saturated steam to enable the temperature and the pressure of the saturated steam to rise, and then the saturated steam after temperature rise and pressure rise is conveyed to the top of the shell pass of the vertical falling-film evaporator.
Specifically, the method comprises a distilled water recovery step, wherein the distilled water recovery step comprises the following steps:
steam in the shell pass of the vertical falling-film evaporator is condensed into distilled water outside a heat exchange tube of the vertical falling-film evaporator, and the distilled water is recycled into a distilled water tank.
Specifically, the recovered distilled water is sent to the preheater, where the residual temperature of the recovered distilled water is heat-exchanged with the dope in the preheating step to preheat the dope.
Specifically, processing system includes raw liquor tank, pre-heater, evaporimeter, vapor compressor, hydrocyclone, the play liquid end of raw liquor tank with the first feed liquor end of pre-heater is connected, the first play liquid end of pre-heater with the bottom sap cavity of evaporimeter is connected, the liquid that the bottom sap cavity stored up passes through the circulating pump sending extremely in the tube side of evaporimeter, vapor compressor's inlet end and the end of giving vent to anger respectively with the shell side of evaporimeter is connected, the bottom sap cavity with hydrocyclone's feed liquor end is connected, hydrocyclone's first play liquid end with the feed liquor end of circulating pump is connected.
Specifically, the processing system includes the swirler intake pump, the inlet end of swirler intake pump with the bottom liquid chamber is connected, the play liquid end of swirler intake pump with hydrocyclone's inlet end is connected.
Specifically, the treatment system comprises a concentrate tank, and a second liquid inlet end of the concentrate tank is connected with a second liquid outlet end of the hydrocyclone.
Specifically, the processing system includes the stoste intake pump, the play liquid end of stoste jar with the feed liquor end of stoste intake pump is connected, the play liquid end of stoste intake pump with the first feed liquor end of pre-heater is connected.
Compared with the prior art, the invention has the beneficial effects that:
the concentration of the seed crystals in the circulating liquid (in the bottom liquid cavity) of the evaporator is lower and lower along with the discharge of the concentrated liquid and the entrance of new raw liquid wastewater. In order to maintain the concentration balance of the seed crystals in the evaporator, when the concentration is discharged, a part of the concentrated solution in the evaporator enters the hydrocyclone, the seed crystals are separated from the concentrated solution under the action of centrifugal force and are recycled in the evaporator for recycling. And discharging the concentrated solution from which the seed crystals are removed into a concentrated solution tank. Wherein, the concentrated solution outlet and the liquid outlet end of the hydrocyclone are both provided with flow measuring devices, and the balance of the crystal seeds in the circulating liquid (in the bottom liquid cavity) can be maintained by regulating and controlling the discharge amount of the concentrated solution and recovering the discharge amount of the crystal seed concentrated solution after the system is stably operated.
In the process of evaporation concentration, although the waste water is continuously concentrated and reduced, the seed crystal balance in the circulating liquid (in the bottom liquid cavity) is effectively maintained, and the inner wall of the bottom liquid cavity is not easy to scale, so that the working performance of the evaporator is maintained.
Drawings
FIG. 1 is a schematic diagram of a high-salt-content wastewater reduction treatment system applied to a thermal power plant.
In the figure: 1. an evaporator; 101. a bottom liquid chamber; 2. a vapor compressor; 3. a circulation pump; 4. a swirler intake pump; 5. a hydrocyclone; 6. a stock solution tank; 7. a stock solution feed pump; 8. a preheater; 9. a distilled water tank; 10. a distilled water pump; 11. a concentrated solution tank; 12. a concentrated liquid pump; 14. and a non-condensable gas outlet.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and the detailed description, and it should be noted that any combination of the embodiments or technical features described below can be used to form a new embodiment without conflict.
The utility model provides a be applied to high salt waste water minimizing treatment system that contains of thermal power plant, includes stock solution jar 6, pre-heater 8, evaporimeter 1, vapor compressor 2, hydrocyclone 5. The liquid outlet end of the raw liquid tank 6 is connected with the first liquid inlet end (A in the figure) of the preheater 8, and the first liquid outlet end (B in the figure) of the preheater 8 is connected with the bottom liquid cavity 101 of the evaporator 1. The liquid stored in the bottom liquid chamber 101 is pumped into the tube side of the evaporator 1 by the circulation pump 3. The air inlet end and the air outlet end of the vapor compressor 2 are respectively connected with the shell side of the evaporator 1. The bottom liquid cavity 101 is connected with the liquid inlet end of the hydrocyclone 5, and the first liquid outlet end (in the figure, C) of the hydrocyclone 5 is connected with the liquid inlet end of the circulating pump 3.
Specifically, the treatment system comprises a stock solution inlet pump 7, the liquid outlet end of the stock solution tank 6 is connected with the liquid inlet end of the stock solution inlet pump 7, and the liquid outlet end of the stock solution inlet pump 7 is connected with the first liquid inlet end (position A in the figure) of the preheater 8.
Specifically, the treatment system comprises a distilled water tank 9, and the liquid inlet end of the distilled water tank 9 is connected with the bottom of the shell pass of the evaporator 1.
Specifically, the treatment system comprises a distilled water pump 10, wherein the liquid inlet end of the distilled water pump 10 is connected with the liquid outlet end of the distilled water tank 9, and the liquid outlet end of the distilled water pump 10 is connected with the second liquid inlet end (position E in the figure) of the preheater 8.
Specifically, the treatment system comprises a cyclone water inlet pump 4, wherein the liquid inlet end of the cyclone water inlet pump 4 is connected with the bottom liquid cavity 101, and the liquid outlet end of the cyclone water inlet pump 4 is connected with the liquid inlet end of the hydrocyclone 5.
Specifically, the treatment system comprises a concentrated solution tank 11, and a first liquid inlet end (in the figure, F) of the concentrated solution tank 11 is connected with a liquid outlet end of the circulating pump 3.
Specifically, a second liquid inlet end (at H in the figure) of the concentrated liquid tank 11 is connected with a second liquid outlet end (at K in the figure) of the hydrocyclone 5.
Specifically, the treatment system comprises a concentrated solution pump 12, and the liquid inlet end of the concentrated solution pump 12 is connected with the liquid outlet end of the concentrated solution tank 11.
Specifically, the evaporator 1 is a vertical falling film evaporator.
Specifically, the shell side of the evaporator 1 is provided with a non-condensable gas outlet 14.
The working principle of the processing system of the application is as follows:
the waste water preheated by the preheater 8 enters the bottom liquid cavity 101 of the evaporator 1, and is sent into the heat exchange tube (tube side) along with the circulating liquid by the circulating pump 3 to exchange heat with the steam outside the tube (in the shell side). Through continuous cyclic heating, the waste water gradually becomes thick, and after the thick liquid reaches the design temperature, partial thick liquid is directly discharged from the bottom liquid cavity 101 and enters the thick liquid tank 11. Along with the discharge of the concentrated solution, the liquid level of the bottom liquid cavity 101 descends, and the raw liquid inlet pump 7 adjusts the water inlet flow to replenish water for the evaporator 1.
The concentration of the seed crystals in the circulating liquid of the evaporator 1 (in the bottom liquid chamber 101) will be lower and lower as the concentrate is discharged and new raw liquid wastewater enters. In order to maintain the seed concentration balance in the evaporator 1, when discharging the concentrated solution, a part of the concentrated solution in the evaporator 1 enters the hydrocyclone 5, and the seed is separated from the concentrated solution under the action of centrifugal force and recycled to the evaporator 1 for recycling. The seed crystal-removed concentrate is discharged into the concentrate tank 11. Wherein, the concentrated solution outlet and the liquid outlet end of the hydrocyclone 5 are both provided with flow measuring devices (not shown in the figure), and the balance of the seed crystals in the circulating liquid can be maintained by regulating and controlling the discharge amount of the concentrated solution and the discharge amount of the recycled seed crystal concentrated solution after the system is stably operated.
The high-salinity wastewater of the thermal power plant has complex components, and the wastewater contains ions which are easy to crystallize into scales, such as carbonate, sulfate radicals, calcium ions, magnesium ions and the like. When the waste water is evaporated and gradually becomes thick, carbonate, sulfate and the like can be separated out from the thick solution and adhere to the wall surface of the heat exchange tube, and scale is accumulated. Suitable seeds are added to the evaporator 1 and maintained in circulation within the evaporator 1. When the solution is close to saturation, calcium carbonate, calcium sulfate and the like are separated out and preferentially grow on the crystal seeds in the solution, so that the crystal seeds are prevented from growing and scaling on the heat exchange tubes of the evaporator 1, and double salts cannot be formed. After the wastewater is concentrated to a certain degree, the concentration is discharged according to the data of boiling point temperature rise, evaporated water amount and the like, a part of concentrated solution is discharged and sent into the hydrocyclone 5, and the hydrocyclone 5 separates the seed crystal from the concentrated solution through centrifugal force and recycles the seed crystal to the evaporator 1, so that the stability of the seed crystal in the system is maintained.
The crystal seed method prevents scaling evaporation, and overcomes the limit of low-solubility compound saturation in the traditional evaporation process; by controlling the circulation amount and discharge amount, controlling the concentration of suspended matters in the concentrated solution and the temperature rise of a boiling point, establishing and maintaining the concentration of crystal seeds in the wastewater circulation process of the evaporator 1, precipitating calcium carbonate, calcium sulfate and the like on the crystal seeds of the circulation solution instead of the wall surface of an evaporator tube, and preventing the generation of scale by changing the production position of crystals. Meanwhile, the seed crystal only needs to be put in through water inlet or a small amount of the seed crystal is put in the evaporator 1 when the evaporation is started, the seed crystal can be recycled in the system, repeated putting is not needed, and the operation cost cannot be increased.
Saturated steam (the temperature is 90-100 ℃) generated by the evaporation of the waste water in the evaporator 1 is sent into the steam compressor 2, works through the steam compressor 2, the temperature and the pressure are increased, the saturated steam enters the upper shell pass of the evaporator 1, and the waste water in the tube pass is heated. The steam is condensed into distilled water outside the pipe, flows into a distilled water tank 9, and is sent to a preheater 8 through a distilled water pump 10 to heat the wastewater stock solution, and the waste heat in the distilled water is recovered.
A reduction treatment method for high-salt-content wastewater of a thermal power plant is applied to a wastewater treatment system, and comprises the following steps:
seed crystal adding step: adding a proper amount of seed crystals to the vertical falling film evaporator;
preheating: the stock solution is sent to a preheater 8 for preheating, and then the preheated stock solution is sent to a vertical falling-film evaporator;
and (3) an evaporation step: circularly evaporating and concentrating the stock solution in a vertical falling-film evaporator;
and (3) grain recovery: and (3) conveying the concentrated solution to a hydrocyclone 5, separating the seed crystals by the hydrocyclone 5, sending the separated seed crystals back to the vertical falling-film evaporator, and sending the concentrated solution from which the seed crystals are separated to a concentrated solution tank 11.
Specifically, in the preheating step, the stock solution is preheated to 55-65 ℃.
Specifically, in the evaporation step, the evaporation temperature of the vertical falling-film evaporator is 90-100 ℃.
Specifically, the method comprises a steam pressurizing step, wherein the steam pressurizing step comprises the following steps:
saturated steam generated by the work of the vertical falling-film evaporator is sent to the steam compressor 2, the steam compressor 2 applies work to the saturated steam to increase the temperature and the pressure of the saturated steam, and then the saturated steam after being heated and pressurized is sent to the top of the shell pass of the vertical falling-film evaporator.
Specifically, the method comprises a distilled water recovery step, wherein the distilled water recovery step comprises the following steps:
steam in the shell pass of the vertical falling-film evaporator is condensed into distilled water outside a heat exchange tube of the vertical falling-film evaporator, and the distilled water is recycled into a distilled water tank 9.
Specifically, the recovered distilled water is sent to the preheater 8, and in the preheater 8, the residual temperature of the recovered distilled water is heat-exchanged with the dope in the preheating step to preheat the dope.
The above embodiments are only preferred embodiments of the present invention, and the protection scope of the present invention is not limited thereby, and any insubstantial changes and substitutions made by those skilled in the art based on the present invention are within the protection scope of the present invention.
Claims (10)
1. A reduction treatment method for high-salt-content wastewater of a thermal power plant is applied to a wastewater treatment system, and is characterized by comprising the following steps:
seed crystal adding step: adding a proper amount of seed crystals to the vertical falling film evaporator;
preheating: the stock solution is sent to a preheater for preheating, and then the preheated stock solution is sent to a vertical falling-film evaporator;
and (3) an evaporation step: circularly evaporating and concentrating the stock solution in a vertical falling-film evaporator;
and (3) grain recovery: and (3) conveying the concentrated solution to a hydrocyclone, separating the seed crystals by the hydrocyclone, sending the separated seed crystals back to the vertical falling-film evaporator, and sending the concentrated solution from which the seed crystals are separated to a concentrated solution tank.
2. The processing method according to claim 1, characterized in that: in the preheating step, the stock solution is preheated to 55-65 ℃.
3. The processing method according to claim 1, characterized in that: in the evaporation step, the evaporation temperature of the vertical falling-film evaporator is 90-100 ℃.
4. The processing method according to claim 1, characterized in that: comprises a steam pressurizing step, wherein the steam pressurizing step comprises the following steps:
saturated steam generated by the work of the vertical falling-film evaporator is sent to a steam compressor, the steam compressor applies work to the saturated steam to enable the temperature and the pressure of the saturated steam to rise, and then the saturated steam after temperature rise and pressure rise is conveyed to the top of the shell pass of the vertical falling-film evaporator.
5. The processing method according to claim 1, characterized in that: comprises a distilled water recovery step, wherein the distilled water recovery step comprises the following steps:
steam in the shell pass of the vertical falling-film evaporator is condensed into distilled water outside a heat exchange tube of the vertical falling-film evaporator, and the distilled water is recycled into a distilled water tank.
6. The processing method according to claim 5, characterized in that: the recovered distilled water is sent to the preheater where the residual temperature of the recovered distilled water is heat-exchanged with the dope in the preheating step to preheat the dope.
7. The processing method according to claim 1, characterized in that: including raw liquor tank, pre-heater, evaporimeter, steam compressor, hydrocyclone, the play liquid end of raw liquor tank with the first feed liquor end of pre-heater is connected, the first play liquid end of pre-heater with the bottom sap cavity of evaporimeter is connected, the liquid that the bottom sap cavity stored up passes through the circulating pump and arrives in the tube side of evaporimeter, steam compressor's inlet end and the end of giving vent to anger respectively with the shell side of evaporimeter is connected, the bottom sap cavity with hydrocyclone's feed liquor end is connected, hydrocyclone's first play liquid end with the feed liquor end of circulating pump is connected.
8. The processing method according to claim 7, characterized in that: the treatment system comprises a cyclone water inlet pump, wherein the liquid inlet end of the cyclone water inlet pump is connected with the bottom liquid cavity, and the liquid outlet end of the cyclone water inlet pump is connected with the liquid inlet end of the hydrocyclone.
9. The processing method according to claim 7, characterized in that: the treatment system comprises a concentrated solution tank, and a second liquid inlet end of the concentrated solution tank is connected with a second liquid outlet end of the hydrocyclone.
10. The processing method according to claim 7, characterized in that: the treatment system comprises a stock solution inlet pump, wherein the liquid outlet end of the stock solution tank is connected with the liquid inlet end of the stock solution inlet pump, and the liquid outlet end of the stock solution inlet pump is connected with the first liquid inlet end of the preheater.
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| CN202010222584.2A CN111494974A (en) | 2020-03-26 | 2020-03-26 | High-salinity wastewater reduction treatment method applied to thermal power plant |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112274957A (en) * | 2020-10-30 | 2021-01-29 | 张家港市蓝鸟机械有限公司 | Hemp oil falling film evaporator |
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