CN114702184B - High-salt high-organic matter wastewater treatment device and method - Google Patents
High-salt high-organic matter wastewater treatment device and method Download PDFInfo
- Publication number
- CN114702184B CN114702184B CN202210366432.9A CN202210366432A CN114702184B CN 114702184 B CN114702184 B CN 114702184B CN 202210366432 A CN202210366432 A CN 202210366432A CN 114702184 B CN114702184 B CN 114702184B
- Authority
- CN
- China
- Prior art keywords
- salt
- distillation
- wastewater
- treatment
- adsorption tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
Abstract
The invention discloses a high-salt high-organic matter wastewater treatment device and method, and belongs to the technical field of wastewater treatment. The device comprises: a water storage tank; the liquid inlet of the distillation kettle is connected with the water storage tank; the liquid inlet of the renewable adsorption tower is connected with the distillation residue liquid outlet of the distillation kettle; the liquid inlet of the reduced pressure rectifying tower is connected with the distillation liquid outlet of the distillation kettle, and the reduced pressure rectifying tower is connected with the water storage tank; the serial multi-effect evaporator consists of 3 evaporators which are connected in series, and a liquid inlet of the serial multi-effect evaporator is connected with a liquid outlet of the renewable adsorption tower; and the first material pool is connected with a discharge port of the serial multi-effect evaporator. The invention also provides a method for treating the high-salt high-organic wastewater by the device, which can realize standard discharge of the wastewater after distillation, rectification, adsorption and multiple-effect treatment of the high-salt high-organic wastewater, and realize recycling of crystalline inorganic salt without subsequent biochemical treatment.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a high-salt high-organic wastewater treatment device and method.
Background
The chemical industry may use some organic salts during production, for example: methyl bromide triphenylphosphine, methyl chloride triphenylphosphine, potassium tert-butoxide, sodium tert-butoxide, etc. After the organic salts participate in the reaction, chemical wastewater with high salt content (mass fraction is 5% -20%) and high organic matter content (COD >180000 mg/L) is brought. The treatment of high-salt and high-organic wastewater generally adopts a dilution method to reduce the salt content of the wastewater, but the discharge of the wastewater after the salt content is reduced can also cause environmental deterioration and even cause salinization of soil and watershed. In addition, the organic matters in the wastewater often contain benzene ring organic matters and halogenated hydrocarbon organic matters, have poor biodegradability, have higher biotoxicity and have larger environmental safety hazards.
The traditional method for treating the high-salt high-organic wastewater comprises the following steps: (1) The method is used for treating the wastewater after dilution, so that the total discharge amount of the wastewater of enterprises is increased, and meanwhile, fenton oxidation, iron-carbon micro-electrolysis, catalytic oxidation and other technologies are carried out, and are limited by factors such as organic matters in the wastewater, method conditions, treatment cost and the like, so that the treated effluent still contains partial refractory organic matters, and the environment is also adversely affected in the later stage. (2) The energy consumption required in the processing of the method is high, and the salt generated after concentration belongs to dangerous waste and is difficult to process. For example, CN105461157a discloses a zero-emission method for high-salt high-organic industrial wastewater, which adopts a mode of 'submerged membrane bioreactor + nanofiltration + high-efficiency reverse osmosis + membrane distillation + evaporative crystallization' to treat the high-salt high-organic industrial wastewater. While the method solves the problem of wastewater discharge and simultaneously recovers water resources to the maximum extent, and basically realizes zero discharge of high-salt high-organic matter industrial wastewater, nanofiltration concentrated water generated in the treatment process of the method is difficult to further treat, and nanofiltration membranes are easy to pollute, so that the input cost is increased. (3) Incineration treatment is carried out on the high-salt high-organic matter wastewater, and an incinerator is adopted to carry out incineration treatment, so that organic matters in the wastewater are removed, and finally, the wastewater is reduced to generate salt-containing hazardous waste. For example, CN201110227902.5 discloses a method for treating wastewater with high salt and high organic content, which adopts an extractant to extract and phase-separate organic matters in the wastewater, the water phase obtained after phase-separation is distilled and dried to obtain mixed salt, and the organic phase obtained after phase-separation is incinerated. However, the burning of the tail gas is a difficult problem for many enterprises. The incineration treatment requires less than 10% salt in the wastewater and is no longer applicable to higher salts. If the salt is diluted to a suitable range, the organic concentration tends to be too low to facilitate combustion. Even if the incineration requirement is met, the cost of treating the wastewater is still high. And aerosol can be generated in the incineration process, so that the difficulty is increased for subsequent tail gas treatment, and meanwhile, the waste heat boiler is often blocked by the aerosol. The core of the incineration treatment is to remove organic matters in water, the incineration process is used for preventing energy consumption, and on the other hand, a large amount of waste gas is generated, which is contrary to the aim of energy conservation and emission reduction. These treatment technologies, on the one hand, do not reduce the emission of pollutants in the environment, but rather increase the emission, and on the other hand, the development of many chemical enterprises is greatly limited.
Although the method for treating the high-salt high-organic matter industrial wastewater is disclosed, the problems of high equipment input cost or process operation cost, insufficient removal of organic matters, no effective utilization of inorganic salt resources and the like still exist. Therefore, how to develop an effective high-salt high-organic matter industrial wastewater treatment method, which not only can remove organic matters with complex components and difficult treatment, but also can realize the effective utilization of inorganic salt resources, and has extremely high value.
Disclosure of Invention
The invention aims to provide a high-salt high-organic matter wastewater treatment device and a high-salt high-organic matter wastewater treatment method, which can remove organic matters with complex components and difficult treatment and can realize effective utilization of inorganic salt resources.
In one aspect, the present invention relates to a high-salt high-organic matter wastewater treatment apparatus comprising: a water storage tank; the liquid inlet of the distillation kettle is connected with the water storage tank; the liquid inlet of the renewable adsorption tower is connected with the distillation residue liquid outlet of the distillation kettle; the liquid inlet of the reduced pressure rectifying tower is connected with the distillation liquid outlet of the distillation kettle, and the reduced pressure rectifying tower is connected with the water storage tank; the serial multi-effect evaporator consists of 3 evaporators which are connected in series, and a liquid inlet of the serial multi-effect evaporator is connected with a liquid outlet of the renewable adsorption tower; and the first material pool is connected with a discharge port of the serial multi-effect evaporator.
In the high-salt high-organic matter wastewater treatment device provided by the invention, one side of the renewable adsorption tower is provided with the regeneration and activation equipment, and the regeneration and activation equipment comprises a leaching tank, a leaching liquor distillation kettle and a second material pool.
Further, in the high-salt high-organic matter wastewater treatment device provided by the invention, the leaching tank is connected with the liquid inlet of the renewable adsorption tower; the liquid inlet of the eluent distillation kettle is connected with the discharge port of the renewable adsorption tower, and the liquid outlet is connected with the liquid inlet of the eluent tank; the second material pool is connected with a discharge port of the leaching liquor distillation kettle.
In another aspect, the present invention relates to a method for treating high-salt and high-organic wastewater, wherein the high-salt and high-organic wastewater is treated by the high-salt and high-organic wastewater treatment device.
Further, in the method for treating the high-salt and high-organic matter wastewater, the salt content in the high-salt and high-organic matter wastewater is 5-20wt% and the COD concentration is 180000-32000 mg/L.
Further, the method for treating the high-salt high-organic matter wastewater provided by the invention comprises the following steps: the high-salt high-organic matter wastewater is sent into a distillation kettle 2 from a water storage tank 1 for distillation treatment, and distilled volatile organic matters enter a reduced pressure rectifying tower 4 for rectification recovery treatment; residual liquid in the distillation kettle 2 enters a renewable adsorption tower 3 to remove residual organic matters in the wastewater, and the wastewater after adsorption treatment enters a serial multi-effect evaporator 5 through an outlet of the renewable adsorption tower 3 to be evaporated, crystallized and dehydrated; and (3) recovering water evaporated by the serial multi-effect evaporator 5, and collecting inorganic salt after crystallization treatment in the first material pool 6.
Further, the method for treating the high-salt high-organic matter wastewater provided by the invention further comprises a regeneration and activation treatment, wherein the regeneration and activation treatment comprises the following steps: stopping feeding after the renewable adsorption tower 3 is saturated in adsorption, and performing regeneration activation treatment on the renewable adsorption tower 3; slowly adding the leaching solvent in the leaching tank 7 into the renewable adsorption tower 3, leaching out the organic matters adsorbed in the renewable adsorption tower 3, introducing the leached leaching solution into the leaching solution distillation kettle 8 for distillation recovery treatment, and introducing the distilled residual liquid obtained by the distillation recovery treatment into the second material pool 9 for treatment.
Further, in the method for treating high-salt and high-organic wastewater, the operation temperature of the distillation kettle is 50-90 ℃, and the operation pressure is 0.05-0.1 MPa; the operation temperature of the vacuum rectifying tower is 50-90 ℃, the operation pressure is 0.05-0.1 MPa, and the reflux ratio of the tower top is 0.2-5; the operation temperature of the eluent distillation kettle is 50-110 ℃, and the operation pressure is 0.05-0.1 MPa.
Further, in the method for treating high-salt and high-organic matter wastewater, the operating temperatures of the 3 evaporators connected in series with the multiple-effect evaporators from the liquid inlet to the liquid outlet are 85-95 ℃, 75-85 ℃ and 65-75 ℃ in sequence; the operating pressure of any one of the evaporators is 0.05-0.5 MPa.
In the method for treating the high-salt and high-organic matter wastewater, the eluent in the leaching tank is any one or more of water, dichloromethane, chloroform, carbon tetrachloride, methanol and ethanol, and the usage amount of the eluent is 1-5 times of the effective volume of the renewable adsorption tower.
The method comprises the steps of feeding high-salt high-organic wastewater to be treated into a distillation kettle from a water storage tank through a pipeline for distillation treatment, and feeding distilled volatile organic matters into a reduced pressure distillation tower through a pipeline for distillation recovery treatment; residual liquid in the distillation still enters a renewable adsorption tower to remove residual organic matters in the wastewater, and the wastewater after adsorption treatment enters a multi-effect evaporator in series through an outlet of the renewable adsorption tower to be evaporated, crystallized and dehydrated; the evaporated water can reach the discharge standard, and the inorganic salt after crystallization treatment flows into a material pool, so that the aim of recycling the high-salt and high-organic wastewater is fulfilled. Thus, the invention further claims the application of the method in the treatment of high-salt and high-organic wastewater.
Compared with the prior art, the invention has the following beneficial effects or advantages:
the invention provides a high-salt high-organic matter wastewater treatment device and a method, wherein the device and the method distill and separate volatile organic matters in high-salt high-organic matter wastewater through distillation treatment, and the separated volatile organic matters enter a vacuum rectifying tower for rectification treatment, and the rectified organic matters are recovered and reused; allowing the residual liquid in the distillation kettle to enter an adsorption device, and adsorbing and removing a small amount of residual organic components in the residual liquid; and (3) performing evaporation crystallization water removal on the inorganic salt wastewater subjected to the adsorption treatment by using a multi-effect evaporator. The device and the method realize innocent treatment of high-salt high-organic wastewater, the evaporated water reaches the discharge standard, and inorganic salt in the wastewater can be crystallized to obtain inorganic salt with higher purity for recycling.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of a high-salt and high-organic matter wastewater treatment device provided by the invention, wherein in the diagram, 1 is a water storage tank, 2 is a distillation kettle, 3 is a renewable adsorption tower, 4 is a reduced pressure rectifying tower, 5 is a serial multi-effect evaporator, 6 is a first material pool, 7 is a leaching tank, 8 is a leaching solution distillation kettle, and 9 is a second material pool.
Description of the embodiments
The following describes the technical aspects of the present invention with reference to examples, but the present invention is not limited to the following examples.
Examples
The embodiment provides a treatment and recovery process of high-salt high-organic wastewater.
As shown in fig. 1, the water storage tank 1 is filled with high-salt and high-organic wastewater to be treated. The distillation still 2 is connected with a liquid inlet of a vacuum rectification tower 4 through a distillation liquid outlet, and the vacuum rectification tower 4 is used for rectifying volatile organic matters. The vacuum rectifying tower 4 and the water storage tank 1 form a loop, volatile organic matters distilled by the vacuum rectifying tower 4 are recovered, and the distilled residual liquid flows back to the water storage tank 1 to be treated. The distillation still 2 is connected with a liquid inlet of a renewable adsorption tower 3 through a distillation residue liquid outlet, and the renewable adsorption tower is used for adsorbing residual organic matters in the distillation residue liquid. The liquid outlet of the renewable adsorption tower 3 is connected with the liquid inlet of the serial multi-effect evaporator 5, and the serial multi-effect evaporator 5 is used for distilling water in the wastewater. The serial multi-effect evaporator 5 is formed by connecting a first evaporator 5-1, a second evaporator 5-2 and a third evaporator 5-3 in series respectively. The discharge port of the multi-effect evaporator 5 is connected with a first material pool 6, and the first material pool 6 is used for recovering the inorganic salt after evaporation and crystallization.
Illustratively, one side of the regenerable adsorption tower 3 is also provided with regeneration and activation equipment, and the adsorption saturated adsorbent is subjected to leaching regeneration and activation by using a leaching solution, so that the regenerable recycling of the adsorption tower is realized. In particular, the regeneration device comprises a leaching tank 7, a leaching liquor distillation kettle 8 and a second material pool 9. The leaching tank 7 is connected with a liquid inlet of the renewable adsorption tower 3; one side of a discharge port of the renewable adsorption tower 3 is connected with a liquid inlet of the distillation kettle; the liquid outlet of the leaching liquor distillation kettle 8 is connected with the liquid inlet of the leaching tank 7; and a discharge hole of the leacheate distillation kettle 8 is connected with a second material pool 9.
The content of inorganic salt in the high-salt high-organic matter wastewater of the embodiment is 5wt percent, and the COD concentration is 180000mg/L. Wherein the inorganic component is potassium bromide, and the organic component is triphenylphosphine oxide, triphenylphosphine, tetrahydrofuran, and tert-butanol. The organic matter component contains triphenylphosphine oxide 24%, triphenylphosphine 14%, tetrahydrofuran 42% and tert-butanol 20%.
According to the device shown in fig. 1, high-salt high-organic wastewater to be treated is sent into a distillation kettle 2 from a water storage tank 1 for distillation treatment, and distilled volatile organic matters enter a reduced pressure rectifying tower 4 for rectification recovery treatment; residual liquid in the distillation kettle 2 enters a renewable adsorption tower 3 to remove residual organic matters in the wastewater, and the wastewater after adsorption treatment enters a serial multi-effect evaporator 5 through an outlet of the renewable adsorption tower 3 to be evaporated, crystallized and dehydrated; the evaporated water can reach the discharge standard, and the inorganic salt after crystallization treatment flows into the first material pool 6 for recycling. Stopping feeding after the adsorbent in the regenerable adsorption tower 5 is saturated, starting to perform the regeneration and activation treatment of the regenerable adsorption tower 5, slowly adding the eluent in the leaching tank 7 into the regenerable adsorption tower 5, leaching out the organic matters adsorbed in the adsorbent, and allowing the leached eluent to enter the eluent distillation kettle 8 for distillation and recovery treatment; the distilled liquid enters a second material pool 9 to be treated.
The size of the distillation still 2 is as follows: 400 x 1100mm, the effective volume is 500L, the operation temperature is 50-90 ℃, and the operation pressure is 0.05-0.1 MPa. The size of the vacuum rectification column 4 is: 180 x 2000mm, an effective volume of 200L, an operating temperature of 50-90 ℃ and an operating pressure of 0.05-0.1 MPa; the reflux ratio of the top of the tower is 0.2-5. The size of the eluent distillation kettle 8 is as follows: 400 x 1100mm, the effective volume is 500L, the operation temperature is 50-110 ℃, and the operation pressure is 0.05-0.1 MPa. The size of the leaching tank 7 is as follows: 400 x 600mm, effective volume 300L, and methanol as the eluting solvent in the eluting tank. The sizes of the evaporators of the series multi-effect evaporators are as follows: 300 x 800mm, effective volume 200L, operating temperature: the operating temperature of the evaporator 5-1 is 85-95 ℃, the operating temperature of the evaporator 5-2 is 75-85 ℃, the operating temperature of the evaporator 5~3 is 65-75 ℃, and the operating pressure is 0.05-0.5 MPa.
The dimensions of the regenerable adsorption column 5 are: 160 x 280mm, the effective volume is 200L, 200L polystyrene adsorption resin is filled in to adsorb residual organic matters, when the residual liquid with the effective volume which is 3 times that of the renewable adsorption tower is adsorbed, the adsorption tower is in an adsorption saturation or near saturation state, and the regeneration and activation operation is started; wherein, the dosage of the eluent is 1 time of the effective volume of the renewable adsorption tower 3.
Determination after treatment by the method described above:
the COD concentration of the multi-effect distilled water is 32mg/L, the TDS concentration is 18mg/L, the content of volatile organic compounds recovered by rectification is 99.2%, and the content of inorganic salt potassium bromide is 97.4%.
Examples
The embodiment provides a treatment recovery test of high-salt high-organic matter wastewater.
The high-salt and high-organic matter wastewater used in the embodiment has the salt content of 10wt% and the COD concentration of 240000mg/L. Wherein the inorganic component is potassium chloride, and the organic component is triphenylphosphine oxide, triphenylphosphine, tetrahydrofuran and tert-butanol. The organic matter component contains triphenylphosphine oxide 12%, triphenylphosphine 15%, tetrahydrofuran 46% and tert-butanol 27%.
The eluent in this example is a methanol solvent and the amount of the eluent is 3 times the effective volume of the regenerable adsorption tower 3.
Determination after treatment by the method described above:
the COD concentration of the multi-effect distilled water is 44mg/L, and the TDS concentration is 32mg/L; the content of volatile organic compounds recovered by rectification is 98.8 percent, and the content of inorganic salt potassium bromide is 98.2 percent.
Examples
The embodiment provides a treatment recovery test of high-salt high-organic matter wastewater.
The high-salt and high-organic matter wastewater used in the embodiment has the inorganic salt content of 20wt% and the COD concentration of 320000mg/L. Wherein the inorganic component is potassium bromide, and the organic component is triphenylphosphine oxide, triphenylphosphine, diphenylphosphine oxide, tetrahydrofuran, and tert-butanol. The organic salt component comprises 14 percent of triphenylphosphine oxide, 18 percent of triphenylphosphine, 8 percent of diphenylphosphine oxide, 38 percent of tetrahydrofuran and 22 percent of tertiary butanol.
The eluent in this example is methanol solvent and the amount of the eluent is 5 times of the effective volume of the regenerable adsorption tower 3.
Determination after treatment by the method described above:
COD concentration of the multi-effect distilled water is 51mg/L, and TDS concentration is 32mg/L; the content of volatile organic compounds recovered by rectification is 98.5 percent, and the content of inorganic salt potassium bromide is 95.7 percent.
The present invention may be better implemented as described above, and the above examples are merely illustrative of preferred embodiments of the present invention and not intended to limit the scope of the present invention, and various changes and modifications made by those skilled in the art to the technical solution of the present invention should fall within the scope of protection defined by the present invention without departing from the spirit of the design of the present invention.
Claims (8)
1. A high salt high organic matter effluent treatment plant, characterized by comprising:
a water storage tank (1);
the liquid inlet of the distillation kettle (2) is connected with the water storage tank (1);
a liquid inlet of the renewable adsorption tower (3) is connected with a distillation residue liquid outlet of the distillation kettle (2);
the liquid inlet of the reduced pressure rectifying tower (4) is connected with the distillation liquid outlet of the distillation kettle (2), and the reduced pressure rectifying tower (4) is connected with the water storage tank (1);
the serial multi-effect evaporator (5) is formed by connecting 3 evaporators in series, and a liquid inlet of the serial multi-effect evaporator (5) is connected with a liquid outlet of the renewable adsorption tower (3);
the first material pool (6) is connected with a discharge port of the serial multi-effect evaporator (5);
one side of the renewable adsorption tower (3) is provided with a regeneration and activation device, and the regeneration and activation device comprises a leaching tank (7), a leaching solution distillation kettle (8) and a second material pool (9).
2. The high-salt high-organic matter wastewater treatment device according to claim 1, characterized in that the leaching tank (7) is connected with a liquid inlet of the renewable adsorption tower (3);
the liquid inlet of the leaching liquor distillation kettle (8) is connected with the discharge port of the renewable adsorption tower (3), and the liquid outlet is connected with the liquid inlet of the leaching tank (7);
the second material pool (9) is connected with a discharge port of the leacheate distillation kettle (8).
3. A method for treating high-salt and high-organic matter wastewater, which is characterized in that the high-salt and high-organic matter wastewater is treated by the high-salt and high-organic matter wastewater treatment device according to any one of claims 1-2; the high-salt high-organic matter wastewater has a salt content of 5-20wt% and a COD concentration of 180000-32000 mg/L.
4. A method of treating high salt and organic wastewater as claimed in claim 3, comprising: the high-salt high-organic matter wastewater is sent into the distillation kettle (2) through a pipeline from the water storage tank (1) for distillation treatment, and distilled volatile organic matters enter the reduced pressure distillation tower (4) through a pipeline for distillation recovery treatment; residual liquid in the distillation kettle (2) enters the renewable adsorption tower (3) to remove residual organic matters in the wastewater, and the wastewater after adsorption treatment enters the serial multi-effect evaporator (5) through an outlet of the renewable adsorption tower (3) to be evaporated, crystallized and dehydrated; and (3) recovering water evaporated by the serial multi-effect evaporator (5), and collecting inorganic salt after crystallization treatment in the first material pool (6).
5. The method for treating high-salt and high-organic wastewater according to claim 3, further comprising a regeneration activation treatment comprising: stopping feeding after the regenerable adsorption tower (3) is saturated in adsorption, and performing regeneration and activation treatment on the regenerable adsorption tower (3); slowly adding the leaching solvent in the leaching tank (7) into the renewable adsorption tower (3), leaching out organic matters adsorbed in the renewable adsorption tower (3), enabling the leached leaching solution to enter the leaching solution distillation kettle (8) for distillation recovery treatment, and enabling the distilled residual liquid obtained by the distillation recovery treatment to enter a second material pool (9) for treatment.
6. The method for treating high-salt and high-organic matter wastewater according to claim 4, wherein the operation temperature of the distillation still (2) is 50-90 ℃ and the operation pressure is 0.05-0.1 MPa;
the operation temperature of the pressure reduction rectifying tower (4) is 50-90 ℃, the operation pressure is 0.05-0.1 MPa, and the reflux ratio of the tower top is 0.2-5;
the operating temperature of the eluent distillation kettle (8) is 50-110 ℃, and the operating pressure is 0.05-0.1 MPa.
7. The method for treating high-salt and high-organic matter wastewater according to claim 4, wherein the 3 evaporators of the series multi-effect evaporator (5) are sequentially a first evaporator (5-1), a second evaporator (5-2) and a third evaporator (5-3) from a liquid inlet to a liquid outlet; the operation temperature of the first evaporator (5-1) is 85-95 ℃, the operation temperature of the second evaporator (5-2) is 75-85 ℃, and the operation temperature of the third evaporator (5-3) is 65-75 ℃; the operating pressure of any one of the first evaporator (5-1), the second evaporator (5-2) and the third evaporator (5-3) is 0.05-0.5 MPa.
8. The method for treating high-salt and high-organic matter wastewater according to claim 4, wherein the eluent in the leaching tank (7) is any one or more of water, dichloromethane, chloroform, carbon tetrachloride, methanol and ethanol, and the usage amount of the eluent is 1-5 times of the effective volume of the renewable adsorption tower (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210366432.9A CN114702184B (en) | 2022-04-08 | 2022-04-08 | High-salt high-organic matter wastewater treatment device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210366432.9A CN114702184B (en) | 2022-04-08 | 2022-04-08 | High-salt high-organic matter wastewater treatment device and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114702184A CN114702184A (en) | 2022-07-05 |
| CN114702184B true CN114702184B (en) | 2023-09-29 |
Family
ID=82171740
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210366432.9A Active CN114702184B (en) | 2022-04-08 | 2022-04-08 | High-salt high-organic matter wastewater treatment device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114702184B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11226560A (en) * | 1998-02-13 | 1999-08-24 | Hitachi Ltd | Method and device for treating waste liquid or waste water |
| CN104355470A (en) * | 2014-10-11 | 2015-02-18 | 波鹰(厦门)科技有限公司 | Device for recovering glycerinum in high-salinity organic wastewater |
| CN106495384A (en) * | 2016-11-03 | 2017-03-15 | 南京格洛特环境工程股份有限公司 | The technique that a kind of utilization organic contamination high-salt wastewater prepares industrial purified salt |
| CN110054342A (en) * | 2019-05-29 | 2019-07-26 | 山东特保罗环保节能科技有限公司 | A method of product salt is obtained to high organic wastewater processing with high salt |
| CN112174244A (en) * | 2020-09-25 | 2021-01-05 | 西安瑞联新材料股份有限公司 | Device and method for treating medium-low concentration DMF (dimethyl formamide) wastewater |
-
2022
- 2022-04-08 CN CN202210366432.9A patent/CN114702184B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11226560A (en) * | 1998-02-13 | 1999-08-24 | Hitachi Ltd | Method and device for treating waste liquid or waste water |
| CN104355470A (en) * | 2014-10-11 | 2015-02-18 | 波鹰(厦门)科技有限公司 | Device for recovering glycerinum in high-salinity organic wastewater |
| CN106495384A (en) * | 2016-11-03 | 2017-03-15 | 南京格洛特环境工程股份有限公司 | The technique that a kind of utilization organic contamination high-salt wastewater prepares industrial purified salt |
| CN110054342A (en) * | 2019-05-29 | 2019-07-26 | 山东特保罗环保节能科技有限公司 | A method of product salt is obtained to high organic wastewater processing with high salt |
| CN112174244A (en) * | 2020-09-25 | 2021-01-05 | 西安瑞联新材料股份有限公司 | Device and method for treating medium-low concentration DMF (dimethyl formamide) wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114702184A (en) | 2022-07-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10662075B2 (en) | Method and apparatus for the recovery and deep treatment of polluted acid | |
| CN109019634B (en) | Chemical waste salt refining and resource utilization system and method | |
| CN109911918B (en) | Resource utilization method of industrial mixed salt containing organic solvent | |
| CN108793551B (en) | Treatment method and treatment device for high-salt high-COD organic wastewater | |
| CN109437462A (en) | A kind of processing method of pyridine waste water | |
| CN108623067A (en) | Process for treating coal chemical wastewater | |
| CN109516622A (en) | The treatment process of high-salt wastewater in a kind of benzyl alcohol production system | |
| CN102139970B (en) | Recycling method for pure terephthalic acid industrial wastewater | |
| CN114702184B (en) | High-salt high-organic matter wastewater treatment device and method | |
| CN109824193A (en) | Alumina chemical industry Waste acid recovery technology | |
| CN110980847B (en) | Treatment and recovery system and method for waste alkali in methane chloride production | |
| CN113003829A (en) | Treatment method of high-salinity organic wastewater | |
| CN111392946A (en) | Method for recovering 1,3 cyclohexanedione from wastewater containing 1,3 cyclohexanedione | |
| CN104071918B (en) | A kind of pretreating process of Coal Chemical Industry high-concentration sewage | |
| CN114590948A (en) | Harmless treatment and resource utilization process for epoxy resin production wastewater | |
| CN100417634C (en) | Method of separating and recovering fumaric acid and phthalic acid in fumaric acid preparation wastewater | |
| CN113683261B (en) | Treatment method of high-concentration high-salt methanol organic wastewater | |
| CN104128067A (en) | Method for recycling organic solvent and processing residual liquid | |
| CN110183322B (en) | Method for treating low-concentration acetic acid wastewater containing mineral acid salts | |
| CN1858007A (en) | Treating and resourcing method for 4.4-diamido diphenyl propylene-2-disulfonic acid production oxide waste water | |
| CN109824155B (en) | System and method for recycling high-concentration COD (chemical oxygen demand) wastewater | |
| CN102295380A (en) | Processing and recovering method of aromatic nitro-compound wastewater | |
| CN101298441B (en) | Method for reclaiming 1,2- benzoisothiazoline-3-ketone from mother liquor | |
| CN1176026C (en) | Method of treating phenol-containing effluent and recovering resource in 2-methyl-4-chlorophenoxyacetic acid producing process | |
| CN116213406B (en) | Solid waste incineration fly ash treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |