CN111494975A - Be applied to automatic processing system of thermal power plant's high salt waste water that contains - Google Patents
Be applied to automatic processing system of thermal power plant's high salt waste water that contains Download PDFInfo
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- CN111494975A CN111494975A CN202010222931.1A CN202010222931A CN111494975A CN 111494975 A CN111494975 A CN 111494975A CN 202010222931 A CN202010222931 A CN 202010222931A CN 111494975 A CN111494975 A CN 111494975A
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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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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses an automatic treatment system applied to high-salt-content wastewater of a thermal power plant, wherein a liquid outlet end of a raw liquid tank is connected with a liquid inlet end of a raw liquid inlet pump, a liquid outlet end of the raw liquid inlet pump is connected with a first liquid inlet end of a preheater, a first liquid outlet end of the preheater is connected with a bottom liquid cavity of an evaporator, the bottom liquid cavity is connected with a liquid inlet end of a circulating pump, a shell side of the evaporator is provided with a shell side liquid inlet valve, a concentrated liquid tank is provided with a concentrated liquid inlet valve, the shell side liquid inlet valve and the concentrated liquid inlet valve are both connected with a liquid outlet end of the circulating pump, the raw liquid tank is provided with a raw liquid level measuring device, the bottom liquid cavity is provided with a bottom liquid level measuring device, the raw liquid level measuring device and the bottom liquid level, the stock solution inlet pump and the circulating pump are electrically connected with the control device, the bottom liquid cavity is provided with a liquid thermometer, and the shell side liquid inlet valve, the concentrated solution inlet valve and the liquid thermometer are electrically connected with the control device. The invention improves the automation degree of the wastewater treatment system and provides the working efficiency of the wastewater treatment system.
Description
Technical Field
The invention relates to an automatic wastewater treatment system, in particular to an automatic treatment system applied to 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. In the wastewater treatment system in the prior art, all the components cannot cooperate automatically, namely, the automation degree of the wastewater treatment system is low, so that the working efficiency of wastewater treatment is influenced.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide an automatic treatment system for high-salt-content wastewater of a thermal power plant, which can improve the automation degree of the wastewater treatment system.
The purpose of the invention is realized by adopting the following technical scheme:
the utility model provides an automatic processing system for high salt waste water that contains of thermal power plant, includes raw liquor tank, stoste intake pump, pre-heater, evaporimeter, circulating pump, thick liquid jar and controlling means, the play liquid end of raw liquor tank with the inlet end of raw liquor intake pump is connected, the play liquid end of raw liquor intake pump with the first inlet end of pre-heater is connected, the first play liquid end of pre-heater with the bottom liquid chamber of evaporimeter is connected, the bottom liquid chamber with the inlet end of circulating pump is connected, the shell side of evaporimeter is equipped with shell side feed liquor valve, thick liquid jar is equipped with thick liquid feed liquor valve, shell side feed liquor valve with thick liquid feed liquor valve all with the play liquid end of circulating pump is connected, the raw liquor tank is equipped with stoste liquid level measuring device, the bottom liquid chamber is equipped with bottom liquid level measuring device, raw liquor level measuring device bottom liquid level measuring device, The stock solution intake pump with the circulating pump all with the controlling means electricity is connected, the bottom sap cavity is equipped with the liquid thermometer, shell side feed liquor valve, dense solution feed liquor valve with the liquid thermometer all with the controlling means electricity is connected.
Specifically, the treatment system comprises a concentrated liquid pump, wherein a liquid inlet end of the concentrated liquid pump is connected with a liquid outlet end of the concentrated liquid tank, the concentrated liquid tank is provided with a concentrated liquid level measuring device, and the concentrated liquid level measuring device and the concentrated liquid pump are both electrically connected with the control device.
Specifically, the concentrated solution tank is provided with a concentrated solution level measuring device, and the concentrated solution level measuring device and the concentrated solution pump are electrically connected with the control device.
Specifically, the treatment system comprises a hydrocyclone and a hydrocyclone water inlet pump, wherein the bottom liquid cavity is connected with the liquid inlet end of the hydrocyclone water inlet pump, and the liquid outlet end of the hydrocyclone water inlet pump is connected with the liquid inlet end of the hydrocyclone.
Specifically, a second liquid inlet end of the concentrate tank is connected with a second liquid outlet end of the hydrocyclone, and a liquid inlet end of the circulating pump is connected with a first liquid outlet end of the hydrocyclone.
Specifically, the treatment system comprises a distilled water tank, and the liquid inlet end of the distilled water tank is connected with the bottom of the shell pass of the evaporator.
Specifically, the processing system includes the distilled water pump, the inlet end of distilled water pump with the play liquid end of distilled water jar is connected, the play liquid end of distilled water pump with the second inlet end of pre-heater is connected.
Specifically, the treatment system comprises a vapor compressor, and a gas inlet end and a gas outlet end of the vapor compressor are respectively connected with a shell pass of the evaporator.
Specifically, the evaporator is a vertical falling film evaporator.
Specifically, the shell side of the evaporator is provided with a non-condensable gas outlet.
Compared with the prior art, the invention has the beneficial effects that:
the bottom liquid level measuring device (arranged in the bottom liquid cavity) is respectively interlocked with the stock solution inlet pump, the circulating pump and the swirler inlet pump. When the liquid level of the bottom liquid cavity is too high, the stock solution inlet pump stops running; when the liquid level of the bottom liquid cavity is too low, the circulating pump and the cyclone water inlet pump stop running.
Preheating the wastewater by a preheater, and raising the temperature to 55-65 ℃; cooling the high-temperature distilled water by a preheater, and then reducing the temperature from 90-100 ℃ to 40-50 ℃. The preheated waste water enters the bottom liquid cavity, is sent into a heat exchange tube (tube side) together with circulating liquid by a circulating pump, and exchanges heat with steam outside the tube (in a shell side). After continuous cyclic heating, the wastewater is gradually thickened, and after the concentrated solution reaches the preset temperature of a solution thermometer (arranged in a bottom solution cavity), the control device controls the shell-side liquid inlet valve to be closed and controls the concentrated solution inlet valve to be opened, so that part of the concentrated solution is discharged from the bottom solution cavity and enters the concentrated solution tank. Along with the discharge of the concentrated solution, the liquid level of the bottom liquid cavity is lowered to be lower than the liquid level measuring device of the bottom liquid, and the raw liquid inlet pump adjusts the water inflow rate to supplement water for the bottom liquid cavity.
Because stoste intake pump, circulating pump, swirler intake pump, shell side feed liquor valve, thick liquid feed liquor valve are connected with the control system electricity respectively, corresponding water pump or valve can be adjusted according to the real-time status of each part in the effluent disposal system to make each part can cooperate automatically, with the degree of automation that improves effluent disposal system, provide effluent disposal system's work efficiency.
Drawings
FIG. 1 is a schematic diagram of an automated treatment system applied to high-salt-content wastewater of 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 an automatic processing system for high salt waste water that contains of thermal power plant, includes stock solution jar 6, stock solution intake pump 7, pre-heater 8, evaporimeter 1, circulating pump 3, concentrate jar 11 and controlling means. 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 (A in the figure) of the preheater 8. The first liquid outlet end (in the figure, B) of the preheater 8 is connected with the bottom liquid cavity 101 of the evaporator 1. The bottom liquid cavity 101 is connected with the liquid inlet end of the circulating pump 3. The shell side of the evaporator 1 is provided with a shell side liquid inlet valve (P in the figure), the concentrated solution tank 11 is provided with a concentrated solution liquid inlet valve (F in the figure), and the shell side liquid inlet valve and the concentrated solution liquid inlet valve are both connected with the liquid outlet end of the circulating pump 3. The stock solution tank 6 is provided with a stock solution level measuring device (not shown), the bottom solution cavity 101 is provided with a bottom solution level measuring device (not shown), and the stock solution level measuring device, the bottom solution level measuring device, the stock solution inlet pump 7 and the circulating pump 3 are all electrically connected with the control device. The bottom liquid cavity 101 is provided with a liquid thermometer (not shown), and the shell side liquid inlet valve, the concentrated liquid inlet valve and the liquid thermometer are all electrically connected with the control device.
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 concentrate tank 11 is provided with a concentrate level measuring device (not shown), and both the concentrate level measuring device and the concentrate pump 12 are electrically connected to the control device.
Specifically, the treatment system comprises a hydrocyclone 5 and a hydrocyclone inlet pump 4, wherein the bottom liquid cavity 101 is connected with the liquid inlet end of the hydrocyclone inlet pump 4, and the liquid outlet end of the hydrocyclone inlet pump 4 is connected with the liquid inlet end of the hydrocyclone 5.
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, and a liquid inlet end of the circulating pump 3 is connected with a first liquid outlet end (at C in the figure) of the hydrocyclone 5.
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 vapor compressor 2, and the gas inlet end and the gas outlet end of the vapor compressor 2 are respectively connected with the shell side of the evaporator 1.
Specifically, the evaporator 1 is a vertical falling film evaporator 1.
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.
The automatic control principle of the processing system of the application is as follows:
the stock solution level measuring device (arranged in the stock solution tank 6) and the stock solution inlet pump 7 are in interlocking control, and when the water level in the stock solution tank 6 is too low, the stock solution inlet pump 7 stops water inlet.
The bottom liquid level measuring device (arranged in the bottom liquid cavity 101) is respectively interlocked with the stock solution inlet pump 7, the circulating pump 3 and the swirler inlet pump 4. When the liquid level of the bottom liquid cavity 101 is too high, the stock solution inlet pump 7 stops running; when the liquid level in the bottom liquid chamber 101 is too low, the circulating pump 3 and the cyclone water inlet pump 4 stop running.
Preheating the wastewater by a preheater 8, and raising the temperature to 55-65 ℃; the temperature of the high-temperature distilled water is reduced from 90-100 ℃ to 40-50 ℃ after being cooled by the preheater 8. The preheated wastewater enters the bottom liquid cavity 101, is sent into a heat exchange tube (tube side) along with circulating liquid by the circulating pump 3, and exchanges heat with steam outside the tube (in the shell side). After continuous cyclic heating, the wastewater gradually becomes concentrated, and after the concentrated solution reaches the preset temperature of the solution thermometer (arranged in the bottom solution cavity 101), the control device controls the shell-side liquid inlet valve (P in the figure) to be closed and controls the concentrated solution inlet valve (F in the figure) to be opened, so that part of the concentrated solution is discharged from the bottom solution cavity 101 and enters the concentrated solution tank 11. Along with the discharge of the concentrated solution, the liquid level of the bottom liquid cavity 101 drops to be lower than the bottom liquid level measuring device, and the raw liquid inlet pump 7 adjusts the water inlet flow rate to supplement water for the bottom liquid cavity 101.
The concentrated solution tank 11 is provided with a concentrated solution level measuring device, the concentrated solution level measuring device and the concentrated solution pump 12 are in interlocking control, and when the concentrated solution in the concentrated solution tank 11 is higher than a preset liquid level, the control device controls the concentrated solution pump 12 to be started to output the concentrated solution. When the liquid level in the concentrate tank 11 is lower than the predetermined low liquid level, the concentrate pump 12 stops outputting the concentrate.
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. The utility model provides a be applied to automatic processing system of thermal power plant's high salt waste water that contains which characterized in that: the system comprises a raw liquid tank, a raw liquid inlet pump, a preheater, an evaporator, a circulating pump, a concentrated liquid tank and a control device, wherein the liquid outlet end of the raw liquid tank is connected with the liquid inlet end of the raw liquid inlet pump, the liquid outlet end of the raw liquid inlet pump is connected with the first liquid inlet end of the preheater, the first liquid outlet end of the preheater is connected with the bottom liquid cavity of the evaporator, the bottom liquid cavity is connected with the liquid inlet end of the circulating pump, the shell side of the evaporator is provided with a shell side liquid inlet valve, the concentrated liquid tank is provided with a concentrated liquid inlet valve, the shell side liquid inlet valve and the concentrated liquid inlet valve are both connected with the liquid outlet end of the circulating pump, the raw liquid tank is provided with a raw liquid level measuring device, the bottom liquid cavity is provided with a bottom liquid level measuring device, the raw liquid inlet pump and the circulating pump are both electrically connected with the control device, the bottom liquid cavity is provided with a liquid thermometer, and the shell side liquid inlet valve, the concentrated liquid inlet valve and the liquid thermometer are electrically connected with the control device.
2. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 1, is characterized in that: the treatment system comprises a concentrated liquid pump, wherein the liquid inlet end of the concentrated liquid pump is connected with the liquid outlet end of the concentrated liquid tank, the concentrated liquid tank is provided with a concentrated liquid level measuring device, and the concentrated liquid level measuring device and the concentrated liquid pump are electrically connected with the control device.
3. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 2 is characterized in that: the concentrated solution tank is provided with a concentrated solution level measuring device, and the concentrated solution level measuring device and the concentrated solution pump are electrically connected with the control device.
4. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 1 is characterized in that: the treatment system comprises a hydrocyclone and a hydrocyclone water inlet pump, wherein the bottom liquid cavity is connected with the liquid inlet end of the hydrocyclone water inlet pump, and the liquid outlet end of the hydrocyclone water inlet pump is connected with the liquid inlet end of the hydrocyclone.
5. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 4 is characterized in that: and a second liquid inlet end of the concentrated solution tank is connected with a second liquid outlet end of the hydrocyclone, and a liquid inlet end of the circulating pump is connected with a first liquid outlet end of the hydrocyclone.
6. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 1, is characterized in that: the treatment system comprises a distilled water tank, and the liquid inlet end of the distilled water tank is connected with the bottom of the shell pass of the evaporator.
7. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 6, is characterized in that: the treatment system comprises a distilled water pump, wherein the liquid inlet end of the distilled water pump is connected with the liquid outlet end of the distilled water tank, and the liquid outlet end of the distilled water pump is connected with the second liquid inlet end of the preheater.
8. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 1, is characterized in that: the treatment system comprises a vapor compressor, and the gas inlet end and the gas outlet end of the vapor compressor are respectively connected with the shell pass of the evaporator.
9. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 1, is characterized in that: the evaporator is a vertical falling-film evaporator.
10. The automatic treatment system applied to the high-salt-content wastewater of the thermal power plant according to claim 1, is characterized in that: and the shell pass of the evaporator is provided with a non-condensable gas outlet.
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| CN202010222931.1A CN111494975A (en) | 2020-03-26 | 2020-03-26 | Be applied to automatic processing system of thermal power plant's high salt waste water that contains |
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| CN202010222931.1A CN111494975A (en) | 2020-03-26 | 2020-03-26 | Be applied to automatic processing system of thermal power plant's high salt waste water that contains |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104135904A (en) * | 2012-01-19 | 2014-11-05 | 水技术国际公司 | Settling chamber for separation of large, plugging particles upstream of a hydroclone |
| CN205379681U (en) * | 2016-01-29 | 2016-07-13 | 南京科盛环保科技有限公司 | Highly enriched extrinsic cycle MVR evaporimeter |
| CN208182649U (en) * | 2018-04-13 | 2018-12-04 | 江苏和诚制药设备制造有限公司 | The MVR processing equipment of electroplating wastewater |
| CN110451709A (en) * | 2019-08-02 | 2019-11-15 | 江苏中圣高科技产业有限公司 | The processing method of production of polysilicon wastewater zero discharge |
-
2020
- 2020-03-26 CN CN202010222931.1A patent/CN111494975A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104135904A (en) * | 2012-01-19 | 2014-11-05 | 水技术国际公司 | Settling chamber for separation of large, plugging particles upstream of a hydroclone |
| CN205379681U (en) * | 2016-01-29 | 2016-07-13 | 南京科盛环保科技有限公司 | Highly enriched extrinsic cycle MVR evaporimeter |
| CN208182649U (en) * | 2018-04-13 | 2018-12-04 | 江苏和诚制药设备制造有限公司 | The MVR processing equipment of electroplating wastewater |
| CN110451709A (en) * | 2019-08-02 | 2019-11-15 | 江苏中圣高科技产业有限公司 | The processing method of production of polysilicon wastewater zero discharge |
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| Title |
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| 毛志伟等: "《氮氧化物减排》", 31 August 2014, 中国建材工业出版社 * |
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