CN113666559A - Method for recovering high-value organic materials from high-salt high-COD wastewater - Google Patents

Method for recovering high-value organic materials from high-salt high-COD wastewater Download PDF

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CN113666559A
CN113666559A CN202110913280.5A CN202110913280A CN113666559A CN 113666559 A CN113666559 A CN 113666559A CN 202110913280 A CN202110913280 A CN 202110913280A CN 113666559 A CN113666559 A CN 113666559A
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concentration
tank
liquid
negative pressure
wastewater
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蒋良秋
谢伟贤
周伟城
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Guangxi Guigang Lanyueliang Water Treatment Environmental Protection Science & Technology Co ltd
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Guangxi Guigang Lanyueliang Water Treatment Environmental Protection Science & Technology Co ltd
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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
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/046—Treatment of water, waste water, or sewage by heating by distillation or evaporation under vacuum produced by a barometric column
    • 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
    • C02F1/048—Purification of waste water by 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
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/285—Treatment of water, waste water, or sewage by sorption using synthetic organic sorbents
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • 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

A method for recovering high-value organic materials from high-salt high-COD wastewater comprises the following steps: A. feeding the wastewater into a concentration and separation device for primary concentration and separation to obtain primary concentrated solution and primary penetrating fluid; B. performing secondary concentration and separation on the primary penetrating fluid to obtain a secondary concentrated solution and a secondary penetrating fluid; C. sending the secondary penetrating fluid into a concentrator to adsorb organic materials, evaporating the discharged filtrate, recovering inorganic salt crystals in the wastewater, and discharging the condensed water after reaching the standard; D. resolving the adsorbed organic material by using a resolving agent to obtain a high-concentration resolving solution; E. rectifying the high-concentration resolution liquid to obtain a resolving agent and an organic material; F. and (3) carrying out negative pressure evaporation treatment on the organic material, the primary concentrated solution and the secondary concentrated solution obtained by rectification, concentrating and recovering the organic material, and discharging the condensate up to the standard or carrying out secondary adsorption treatment. The method can recover the organic materials in the wastewater, ensure the wastewater to reach the standard and generate considerable economic benefits.

Description

Method for recovering high-value organic materials from high-salt high-COD wastewater
Technical Field
The invention relates to the technical field of waste water environmental protection treatment, in particular to a method for recovering high-value organic materials from waste water with high salt content and high COD content.
Background
A considerable part of wastewater discharged by industries such as medicine, food, electroplating, chemical engineering and the like carries organic raw materials, intermediates and reaction byproducts, and the pollutant components are complex and have high concentration. Because such wastewater not only has a high COD concentration but also contains a high concentration of salts, the traditional biological method is difficult to realize effective treatment. The prior treatment method is to degrade COD components in wastewater by adopting advanced oxidation (mainly comprising Fenton oxidation, ozone catalytic oxidation, photocatalytic oxidation, electrocatalytic oxidation and the like), and then remove salt in the wastewater by negative pressure evaporation, however, a large amount of medicament and catalyst are required to be added in the treatment process to degrade the COD in the wastewater, the treatment cost is very high, a large amount of hazardous waste is generated, and the wastewater is difficult to discharge after reaching the standard.
Disclosure of Invention
The invention aims to provide a method for recovering high-value organic materials from high-salt high-COD wastewater, which is used for completely extracting the organic materials in the wastewater, and recycling the organic materials in the wastewater through material means such as purification, concentration, drying and the like, thereby ensuring that the wastewater is discharged after reaching the standard, generating considerable economic benefit, and realizing the purpose of changing waste into valuable and treating the wastewater with waste.
The technical scheme is as follows:
a method for recovering high-value organic materials from high-salt high-COD wastewater comprises the following steps:
A. first-stage concentration and separation: the wastewater to be treated is sent into a set of concentration and separation device for primary concentration and separation to obtain primary concentrated solution and primary penetrating fluid.
B. Secondary concentration and separation: the first-stage penetrating fluid is sent into another set of concentration and separation device for second-stage concentration and separation to obtain a second-stage concentrated solution and a second-stage penetrating fluid.
C. Organic material adsorption: the secondary penetrating fluid is sent into the enricher to adsorb organic materials, filtrate discharged from the enricher is evaporated by a set of negative pressure evaporator, inorganic salt in the wastewater is crystallized and recovered, and the condensed water is discharged after reaching the standard; the crystallized inorganic salt is centrifuged and dried to obtain solid salt, and a certain economic benefit can be obtained by selling the solid salt, so that part of the treatment cost can be reduced.
D. And (3) organic material analysis: and (4) resolving the organic materials adsorbed by the enricher by using a resolving agent to obtain a high-concentration resolving liquid.
E. Rectifying high-concentration resolution solution: sending the high-concentration resolution liquid to a rectification unit for treatment, separating to obtain a resolution agent and an organic material, and recycling the resolution agent.
F. Concentrating and recycling organic materials: evaporating the organic material, the primary concentrated solution and the secondary concentrated solution obtained by rectification by another set of negative pressure evaporator, concentrating and recovering the organic material, and discharging the condensate liquid after reaching the standard or sending the condensate liquid into an enriching device for secondary adsorption treatment; can deeply remove salt or moisture from the concentrated organic materials, improve the concentration and quality of the recovered materials and improve the gas recovery value. And selecting the drying form and the drying temperature of the drying device and the material of the drying device according to the properties of the dried materials.
Further preferred is: characteristic parameters of the concentration and separation device:
1) the operation mode is as follows: and (4) circulating and concentrating.
2) Controlling the concentration of the concentrated solution: the concentration times are calculated by measuring the treated water quantity and the accumulated flow of penetrating fluid.
3) Operating pressure: 0.3-2.1 MPa.
4) Membrane flux: 5-18LMH (L/m)2.h）。
5) And (3) organic matter purification mode: firstly concentrating and reducing (concentration multiple), adding pure water (the conductivity is less than or equal to 5 uS/cm) pairs
6) Washing the concentrated solution with water to remove impurity components in the concentrated solution.
7) Selecting membrane elements: an appropriate membrane element is selected according to the properties of the organic matter to be extracted.
8) Flow rate on membrane surface: 0.1-6m/s (selected according to the nature of the organic material being extracted).
Further preferred is: characteristic parameters of the enricher:
1) controlling the COD concentration of inlet water: less than or equal to 5000 mg/L.
2) The number of series stages of the exchange columns is as follows: 2-4 stages.
3) The pH value range of the inlet water is as follows: 5-8.
4) Selecting the type of the resin: special adsorption special resin with good selectivity.
5) The filtering speed is as follows: 2-6 m/h.
6) Height of resin filling layer: 1500mm-3000 mm.
Further preferred is: characteristic parameters of the negative pressure evaporator:
1) vacuum degree of the negative pressure evaporator: 0.04-0.08 MPa.
2) Negative pressure evaporator efficiency: single effect or triple effect.
3) Energy-saving device of negative pressure evaporator: the condensed water generated by the negative pressure evaporator exchanges heat with the inlet water through an energy-saving device (plate heat exchanger), and the waste heat in the condensed water is fully recovered, so that the initial temperature of the inlet water is increased, the steam consumption is reduced, and the purpose of energy conservation is achieved.
4) The control mode is as follows: and controlling the conductivity of the condensate as the control standard of the evaporation process.
Further preferred is: analytical characteristic parameters of the organic materials:
1) selecting a resolving agent: 3-4% sodium hydroxide solution or 99% organic solvent, and the analysis agent is selected according to the nature of the analyzed material and the extraction purpose.
2) Collecting the analytic solution: the concentrated solution and the dilute solution are collected in a classified way, the concentrated solution is directly subjected to rectification or negative pressure evaporation, and the dilute solution is subjected to cyclic adsorption.
3) A liquid inlet mode of the desorption liquid: and feeding liquid in a countercurrent mode.
4) Liquid inlet flow rate of the desorption liquid: 3-4 m/h.
5) Temperature of the resolution solution: 15-35 ℃.
6) Water washing flow rate: 4-10 m/h.
Further preferred is: characteristic parameters of the rectifying tower:
1) and selecting a reasonable rectifying tower according to the properties of the separated material and the resolving agent.
2) The material of the rectifying tower is selected according to the properties of the material to be separated and the resolving agent.
3) The gas phase of the rectifying tower exchanges heat with the inlet water of the rectifying tower, and the aim of saving energy in the rectifying process is fulfilled by improving the temperature of the inlet water.
The device for recovering high-value organic materials from high-salt high-COD wastewater comprises a raw water tank, a No. I concentration and separation device, a No. II concentration and separation device and an enrichment device, wherein a water outlet of the raw water tank is connected with the No. I concentration and separation device through a pipeline provided with a No. I circulating pump and a precise filter; a concentrated solution outlet of the No. I concentration and separation device is connected with a concentrated solution tank, and a penetrating solution outlet of the No. I concentration and separation device is connected with a penetrating solution tank; the outlet of the No. I osmotic liquid tank is connected with the No. II concentration and separation device through a pipeline provided with a No. II circulating pump, the concentrated liquid outlet of the No. II concentration and separation device is connected with a concentrated liquid tank, and the osmotic liquid outlet of the No. II concentration and separation device is connected with a No. II osmotic liquid tank; the outlet of the No. II osmotic liquid tank is connected with the water inlet of the enrichment device through a pipeline provided with an osmotic liquid delivery pump; a filtrate port of the enricher is connected with a filtrate box, the filtrate box is connected with a No. I negative pressure evaporator through a pipeline provided with a filtrate delivery pump, a condensation outlet of the No. I negative pressure evaporator is connected with a No. I condensation water tank, and a discharge port of the No. I negative pressure evaporator is connected with a No. I recovery tank; the water inlet of the enricher is also connected with a pure water tank through a pipeline provided with a washing pump, the liquid inlet of the enricher is connected with a resolving agent tank through a pipeline provided with a resolving agent pump, and the liquid outlet of the enricher is connected with a resolving agent tank; the desorption liquid box is connected with a rectifying tower through a pipeline provided with a desorption liquid pump, a rectifying port of the rectifying tower is connected with a desorption agent recovery box, and a discharge port of the rectifying tower is connected with a material box; the material box is connected with a No. II negative pressure evaporator through a pipeline provided with a material conveying pump, a discharge port of the No. II negative pressure evaporator is connected with a No. II recovery box, and a condensation outlet of the No. II negative pressure evaporator is connected with a No. II condensation water tank; the concentrated solution tank is connected with the material tank or the No. II negative pressure evaporator through a pipeline provided with a concentrated solution delivery pump.
Further preferred is: the analytic agent recovery tank is connected with the analytic agent tank through a pipeline provided with an analytic liquid feedback pump.
The pipeline is provided with a conductivity meter, a pressure gauge, a one-way valve, a flowmeter and a manual ball valve according to requirements. The device adopted can be installed and used in the market, wherein the precision filter is used for filtering impurities such as suspended matters in the comprehensive wastewater, and the enriching device is required to be filled with resin for adsorbing noble metal ions.
The method for recovering the high-value organic materials from the high-salt high-COD wastewater comprises the steps of extracting the high-value organic materials in the high-salt high-COD wastewater and converting the high-value organic materials into high-purity products, recycling the organic materials in the wastewater, realizing the maximization of benefits and changing waste into valuable; the COD index in the wastewater directly reaches the standard, the wastewater treatment cost is greatly reduced, and the waste treatment by waste is realized. The popularization and the application of the technology can greatly reduce the treatment cost of the high-salt and high-COD wastewater, completely change the environmental protection treatment mode of the conventional treatment process, which only invests and has no income, realize the environmental protection treatment mode of the waste nutrient wastewater for recycling project investment in the same year, also can generate considerable economic income for environmental protection treatment, and improve the enthusiasm and the motive power of the enterprises for environmental protection and pollution treatment.
Drawings
FIG. 1 is a schematic diagram showing the connection relationship of the apparatus for recovering high-value organic substances;
FIG. 2 is a schematic diagram of the connection relationship of the concentration unit devices;
FIG. 3 is a schematic view showing the connection relationship of the adsorption unit devices;
FIG. 4 is a schematic diagram showing the connection of the filtrate distillation unit apparatus;
FIG. 5 is a schematic view showing the connection relationship between the analytical solution distillation unit devices;
FIG. 6 is a schematic diagram showing the connection of the organic material distillation unit apparatus;
wherein the content of the first and second substances,
Figure 320126DEST_PATH_IMAGE001
a cable floating ball is shown,
Figure 830742DEST_PATH_IMAGE002
the conductivity meter is represented by a conductivity meter,
Figure 813741DEST_PATH_IMAGE003
a pressure gauge is shown to indicate the pressure of the fluid,
Figure 303890DEST_PATH_IMAGE004
a one-way valve is shown,
Figure 587104DEST_PATH_IMAGE005
the flow meter is shown in a schematic representation,
Figure 675146DEST_PATH_IMAGE006
represents a manual ball valve;
the names corresponding to the sequence numbers in the figure are:
1. a raw water tank; 2. a circulating pump I; 3. a precision filter; 4. a No. I concentration and separation device; 5. a concentrated solution tank; 6. a concentrate delivery pump; 7. a permeate tank I; 8. a circulating pump II; 9. no. II concentration and separation device; 10. no. II osmotic fluid tank; 11. a permeate transfer pump; 12. an enricher; 13. a filtrate tank; 14. a filtrate delivery pump; 15. a No. I negative pressure evaporator; 16. a No. I condensed water tank; 17. a No. I recycling bin; 18. no. II recovery box; 19. no. II condensation water tank; 20. no. II negative pressure evaporator; 21. a desorption liquid return pump; 22. a resolving agent recovery box; 23. a material transfer pump; 24. a material box; 25. a rectifying tower; 26. analyzing a liquid pump; 27. a desorption solution tank; 28. a resolver pump; 29. a resolver box; 30. a water washing pump; 31. pure water tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
The following steps are adopted to recover high-value organic materials from the high-salt high-COD wastewater:
A. first-stage concentration and separation: the wastewater to be treated is sent into a set of concentration and separation device for primary concentration and separation to obtain primary concentrated solution and primary penetrating fluid.
B. Secondary concentration and separation: the first-stage penetrating fluid is sent into another set of concentration and separation device for second-stage concentration and separation to obtain a second-stage concentrated solution and a second-stage penetrating fluid.
C. Organic material adsorption: and (3) feeding the secondary penetrating fluid into the enricher to adsorb organic materials, evaporating the filtrate discharged from the enricher by using a set of negative pressure evaporator, crystallizing and recovering inorganic salt in the wastewater, and discharging the condensed water up to the standard.
D. And (3) organic material analysis: and (4) resolving the organic materials adsorbed by the enricher by using a resolving agent to obtain a high-concentration resolving liquid.
E. Rectifying high-concentration resolution solution: sending the high-concentration resolution liquid to a rectification unit for treatment, separating to obtain a resolution agent and an organic material, and recycling the resolution agent.
F. Concentrating and recycling organic materials: and evaporating the organic material, the primary concentrated solution and the secondary concentrated solution obtained by rectification by using another set of negative pressure evaporator, concentrating and recovering the organic material, and discharging the condensate liquid after reaching the standard or sending the condensate liquid into an enriching device for secondary adsorption treatment.
The device for recovering high-value organic materials from high-salt high-COD wastewater comprises a raw water tank 1, a No. I concentration and separation device 4, a No. II concentration and separation device 9 and an enricher 12, wherein a water outlet of the raw water tank 1 is connected with the No. I concentration and separation device 4 through a pipeline provided with a No. I circulating pump 2 and a precision filter 3; a concentrated solution outlet of the No. I concentration and separation device 4 is connected with a concentrated solution tank 5, and a penetrating solution outlet of the No. I concentration and separation device 4 is connected with a penetrating solution tank 7; the outlet of the No. I osmotic liquid tank 7 is connected with the No. II concentration and separation device 9 through a pipeline provided with a No. II circulating pump 8, the concentrated liquid outlet of the No. II concentration and separation device 9 is connected with a concentrated liquid tank 5, and the osmotic liquid outlet of the No. II concentration and separation device 9 is connected with a No. II osmotic liquid tank 10; the outlet of the No. II osmotic liquid tank 10 is connected with the water inlet of the enrichment device 12 through a pipeline provided with an osmotic liquid delivery pump 11; a filtrate port of the enricher 12 is connected with a filtrate box 13, the filtrate box 13 is connected with a No. I negative pressure evaporator 15 through a pipeline provided with a filtrate delivery pump 14, a condensation outlet of the No. I negative pressure evaporator 15 is connected with a No. I condensation water tank 16, and a discharge port of the No. I negative pressure evaporator 15 is connected with a No. I recovery tank 17; the water inlet of the enricher 12 is also connected with a pure water tank 31 through a pipeline provided with a water washing pump 30, the liquid inlet of the enricher 12 is connected with a desorption agent tank 29 through a pipeline provided with a desorption agent pump 28, and the liquid outlet of the enricher 12 is connected with a desorption liquid tank 27; the analytic liquid tank 27 is connected with a rectifying tower 25 through a pipeline provided with an analytic liquid pump 26, a rectifying port of the rectifying tower 25 is connected with an analytic agent recovery tank 22, and a discharge port of the rectifying tower 25 is connected with a material tank 24; the material box 24 is connected with a No. II negative pressure evaporator 20 through a pipeline provided with a material conveying pump 23, a discharge port of the No. II negative pressure evaporator 20 is connected with a No. II recovery box 18, and a condensation outlet of the No. II negative pressure evaporator 20 is connected with a No. II condensation water tank 19; the concentrated solution tank 5 is connected with the material tank 24 or the No. II negative pressure evaporator 20 through a pipeline provided with a concentrated solution delivery pump 6.
The analyzing agent recovery tank 22 is connected to the analyzing agent tank 29 through a pipe to which the analyzing liquid return pump 21 is attached.
Characteristic parameters of the concentration and separation device:
1) the operation mode is as follows: and (4) circulating and concentrating.
2) Controlling the concentration of the concentrated solution: the concentration times are calculated by measuring the treated water quantity and the accumulated flow of penetrating fluid.
3) Operating pressure: 0.3-2.1 MPa.
4) Membrane flux: 5-18LMH (L/m)2.h）。
5) And (3) organic matter purification mode: firstly concentrating and reducing (concentration multiple), adding pure water (the conductivity is less than or equal to 5 uS/cm) pairs
6) Washing the concentrated solution with water to remove impurity components in the concentrated solution.
7) Selecting membrane elements: an appropriate membrane element is selected according to the properties of the organic matter to be extracted.
8) Flow rate on membrane surface: 0.1-6m/s (selected according to the nature of the organic material being extracted).
Characteristic parameters of the enricher:
1) controlling the COD concentration of inlet water: less than or equal to 5000 mg/L.
2) The number of series stages of the exchange columns is as follows: 2-4 stages.
3) The pH value range of the inlet water is as follows: 5-8.
4) Selecting the type of the resin: special adsorption special resin with good selectivity.
5) The filtering speed is as follows: 2-6 m/h.
6) Height of resin filling layer: 1500mm-3000 mm.
Characteristic parameters of the negative pressure evaporator:
1) vacuum degree of the negative pressure evaporator: 0.04-0.08 MPa.
2) Negative pressure evaporator efficiency: single effect or triple effect.
3) Energy-saving device of negative pressure evaporator: the condensed water generated by the negative pressure evaporator exchanges heat with the inlet water through an energy-saving device (plate heat exchanger), and the waste heat in the condensed water is fully recovered, so that the initial temperature of the inlet water is increased, the steam consumption is reduced, and the purpose of energy conservation is achieved.
4) The control mode is as follows: and controlling the conductivity of the condensate as the control standard of the evaporation process.
Analytical characteristic parameters of the organic materials:
1) selecting a resolving agent: 3-4% sodium hydroxide solution or 99% organic solvent, and the analysis agent is selected according to the nature of the analyzed material and the extraction purpose.
2) Collecting the analytic solution: the concentrated solution and the dilute solution are collected in a classified way, the concentrated solution is directly subjected to rectification or negative pressure evaporation, and the dilute solution is subjected to cyclic adsorption.
3) A liquid inlet mode of the desorption liquid: and feeding liquid in a countercurrent mode.
4) Liquid inlet flow rate of the desorption liquid: 3-4 m/h.
5) Temperature of the resolution solution: 15-35 ℃.
6) Water washing flow rate: 4-10 m/h.
Characteristic parameters of the rectifying tower:
1) and selecting a reasonable rectifying tower according to the properties of the separated material and the resolving agent.
2) The material of the rectifying tower is selected according to the properties of the material to be separated and the resolving agent.
3) The gas phase of the rectifying tower exchanges heat with the inlet water of the rectifying tower, and the aim of saving energy in the rectifying process is fulfilled by improving the temperature of the inlet water.
Engineering application case
60m of Guangdong New Material Ltd3Waste water project
Project wastewater quality and drainage standard
1. Quality of waste water
Figure 535655DEST_PATH_IMAGE007
2. Waste water components and content of each component
Figure 203396DEST_PATH_IMAGE008
3. Drainage standard
COD：≤90mg/L。
NH3-N：≤10mg/L。
T-N：≤20mg/L。
pH：6-9。
Third, economic benefits
1. PVPK30 revenue
PVPK300.84t/d is recovered every day, the market price of PVPK30 is calculated according to 30000 yuan/t, and the income per day is as follows:
0.84t/d multiplied by 30000 yuan/t =25200 yuan/d, and the PVPK30 recovered in the project is recycled as raw material by the company.
A yield of 25200 dollars may be generated by recycling PVPK30 each day.
2. Gain of sodium nitrate
1.2t/d of sodium nitrate solid salt can be recovered every day, sodium nitrate is sold according to byproducts, the market price of each ton of sodium nitrate is calculated according to 1000 yuan/t, and the income per day is as follows:
1.2t/d × 1000 yuan/t =1200 yuan/d. The sodium nitrate recovered in the project is sold as a byproduct, and a 1200 yuan gain can be generated by recovering the sodium nitrate every day.
Fourth, the treatment cost
Through the operation data statistics of the project one year, the treatment cost of each ton of wastewater is 68 yuan/t, the amount of the wastewater treated each day is 60t, and the operation cost each day is as follows: 60t × 68/t = 4080/d.
Five, annual economic benefits
[ 25200 yuan/d +1200 yuan/d) -4080 yuan/d ] x 340d/a =7588800 yuan/a.
That is, an economic return of 7588800 yuan/a can be generated by wastewater treatment every year.
Sixth, investment recovery period
The total investment of the project is RMB 6780000 Yuan, and the total investment of the project is recovered one year after the project is implemented.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.

Claims (5)

1. A method for recovering high-value organic materials from high-salt high-COD wastewater is characterized in that: the method comprises the following steps:
A. first-stage concentration and separation: sending the wastewater to be treated into a set of concentration and separation device for primary concentration and separation to obtain primary concentrated solution and primary penetrating fluid;
B. secondary concentration and separation: the first-stage penetrating fluid is sent into another set of concentration and separation device for second-stage concentration and separation to obtain a second-stage concentrated solution and a second-stage penetrating fluid;
C. organic material adsorption: the secondary penetrating fluid is sent into the enricher to adsorb organic materials, filtrate discharged from the enricher is evaporated by a set of negative pressure evaporator, inorganic salt in the wastewater is crystallized and recovered, and the condensed water is discharged after reaching the standard;
D. and (3) organic material analysis: utilizing a resolving agent to resolve the organic materials adsorbed by the enricher to obtain high-concentration resolving liquid;
E. rectifying high-concentration resolution solution: sending the high-concentration resolution liquid to a rectification unit for treatment, separating to obtain a resolution agent and an organic material, and recycling the resolution agent;
F. concentrating and recycling organic materials: and evaporating the organic material, the primary concentrated solution and the secondary concentrated solution obtained by rectification by using another set of negative pressure evaporator, concentrating and recovering the organic material, and discharging the condensate liquid after reaching the standard or sending the condensate liquid into an enriching device for secondary adsorption treatment.
2. The method of claim 1 for recovering high value organic materials from high salt and high COD wastewater, wherein: the concentration and separation device adopts a circulating concentration operation mode, the operation pressure is 0.3-2.1MPa, and the membrane flux is 5-18L/m2.h。
3. The method of claim 1 for recovering high value organic materials from high salt and high COD wastewater, wherein: the vacuum degree of the negative pressure evaporator is 0.04-0.08 MPa.
4. The method of claim 1 for recovering high value organic materials from high salt and high COD wastewater, wherein: the device for recovering high-value organic materials from high-salt high-COD wastewater comprises a raw water tank (1), a No. I concentration and separation device (4), a No. II concentration and separation device (9) and an enrichment device (12), wherein a water outlet of the raw water tank (1) is connected with the No. I concentration and separation device (4) through a pipeline provided with a No. I circulating pump (2) and a precise filter (3); a concentrated solution outlet of the No. I concentration and separation device (4) is connected with a concentrated solution box (5), and a penetrating fluid outlet of the No. I concentration and separation device (4) is connected with a penetrating solution box (7); an outlet of the No. I osmotic liquid tank (7) is connected with a No. II concentration and separation device (9) through a pipeline provided with a No. II circulating pump (8), a concentrated liquid outlet of the No. II concentration and separation device (9) is connected with a concentrated liquid tank (5), and an osmotic liquid outlet of the No. II concentration and separation device (9) is connected with a No. II osmotic liquid tank (10); the outlet of the No. II osmotic liquid tank (10) is connected with the water inlet of the enrichment device (12) through a pipeline provided with an osmotic liquid delivery pump (11); a filtrate port of the enricher (12) is connected with a filtrate box (13), the filtrate box (13) is connected with a No. I negative pressure evaporator (15) through a pipeline provided with a filtrate delivery pump (14), a condensation outlet of the No. I negative pressure evaporator (15) is connected with a No. I condensation water tank (16), and a discharge port of the No. I negative pressure evaporator (15) is connected with a No. I recovery box (17); the water inlet of the enricher (12) is also connected with a pure water tank (31) through a pipeline provided with a water washing pump (30), the liquid inlet of the enricher (12) is connected with a desorption agent tank (29) through a pipeline provided with a desorption agent pump (28), and the liquid outlet of the enricher (12) is connected with a desorption liquid tank (27); the desorption liquid tank (27) is connected with a rectifying tower (25) through a pipeline provided with a desorption liquid pump (26), the rectifying port of the rectifying tower (25) is connected with a desorption agent recovery tank (22), and the discharge port of the rectifying tower (25) is connected with a material tank (24); the material tank (24) is connected with a No. II negative pressure evaporator (20) through a pipeline provided with a material conveying pump (23), a discharge hole of the No. II negative pressure evaporator (20) is connected with a No. II recovery tank (18), and a condensation outlet of the No. II negative pressure evaporator (20) is connected with a No. II condensation water tank (19); the concentrated solution tank (5) is connected with the material tank (24) or the No. II negative pressure evaporator (20) through a pipeline provided with a concentrated solution delivery pump (6).
5. The method of claim 4 for recovering high value organic materials from high salt and high COD wastewater, wherein the method comprises the following steps: the analysis agent recovery box (22) is connected with the analysis agent box (29) through a pipeline provided with an analysis liquid return pump (21).
CN202110913280.5A 2021-08-10 2021-08-10 Method for recovering high-value organic materials from high-salt high-COD wastewater Pending CN113666559A (en)

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WO2019092173A1 (en) * 2017-11-10 2019-05-16 Steeper Energy Aps Recovery system for high pressure processing system
CN109912098A (en) * 2019-04-01 2019-06-21 南京简迪环境工程有限公司 A kind of resin adsorption treatment process of high-salt wastewater containing amine system
CN112456710A (en) * 2020-11-18 2021-03-09 深圳市九牧水处理科技有限公司 Method for recycling high-value materials from chemical wastewater

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2013202604A (en) * 2012-03-29 2013-10-07 Kurita Water Ind Ltd Method and device for treating thiourea containing water
WO2019092173A1 (en) * 2017-11-10 2019-05-16 Steeper Energy Aps Recovery system for high pressure processing system
CN109292882A (en) * 2018-10-11 2019-02-01 陕西蓝深特种树脂有限公司 A method of removing organic matter in haline water
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