CN212864613U - Synthetic leather waste water treatment and DMF recovery system - Google Patents
Synthetic leather waste water treatment and DMF recovery system Download PDFInfo
- Publication number
- CN212864613U CN212864613U CN202021721446.0U CN202021721446U CN212864613U CN 212864613 U CN212864613 U CN 212864613U CN 202021721446 U CN202021721446 U CN 202021721446U CN 212864613 U CN212864613 U CN 212864613U
- Authority
- CN
- China
- Prior art keywords
- tower
- dmf
- stage
- synthetic leather
- water vapor
- 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
Images
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides a synthetic leather waste water treatment and DMF recovery system, synthetic leather waste water that contains DMF gets into the vaporizer after preheating, the synthetic leather waste water that contains DMF in the vaporizer is all vaporized and is got into one-level dehydration tower and carry out the mass transfer separation, the DMF of production, heavy component solution and formic acid get into the second grade rectifying tower, DMF has the dimethylamine foul smell that trace decomposition formed to smuggle in vapor and send out from second grade rectifying tower top in the second grade rectifying tower, vapor condensate after the condensation flows back to the dehydration tower, dimethylamine is not congealed the gas and is sent to tail gas processing apparatus, the DMF at the bottom of the second grade rectifying tower, formic acid and high-boiling substance get into tertiary deacidification tower and carry out the mass transfer separation; a part of water vapor at the outlet of the first-stage water vapor compressor is used as a heat source for the vaporization tank; saturated steam at the outlet of the second-stage water vapor compressor is used as a heat source of a dehydration tower, a DMF refining tower, a deamination tower and an deacidification tower. The whole rectification system adopts negative pressure operation, reduces the temperature required by rectification, and can improve the DMF recovery rate by 3-5% on the basis of the prior art.
Description
Technical Field
The utility model relates to an industry DMF handles, concretely relates to synthetic leather waste water treatment and DMF recovery system.
Background
Polyurethane (PU) synthetic leather mainly comprises a dry method and a wet method, wherein in the dry method production process, a large amount of dimethylformamide (also known as DMF) waste gas is sprayed by water to form a DMF-containing aqueous solution; in the wet production process, the leather is washed by water to dissolve DMF in water to form an aqueous solution containing DMF. The waste water can be recycled after being recovered and purified by the technical means, on one hand, the COD, ammonia nitrogen and total nitrogen content in the waste water can be effectively reduced, so that the waste water can be discharged up to the standard, on the other hand, the production cost can be reduced, and the economic value is improved.
DMF recovered in the market at present mainly provides heat for each rectifying tower by a multi-effect rectifying process, mainly a two-tower rectifying process, a three-tower rectifying process, an energy-saving three-tower rectifying process and an immature low-temperature heat pump rectifying process, and raw steam is used as a heat source. The two-tower rectification mainly uses low-pressure steam or heat conducting oil as a heat medium and consists of two towers of atmospheric concentration and reduced pressure rectification, the recovery technology is relatively backward, the energy consumption is high, and the quality of DMF is unstable and the recovery rate is low by adopting a conventional instrument control system.
The three-tower rectification adopts the decompression concentration and normal pressure rectification technologies, medium pressure steam or heat conducting oil is used as a heat source, and energy is utilized in a gradient manner, so that the energy consumption is reduced. The decompression concentration greatly reduces the decomposition rate of DMF, the DMF recovery rate can reach 90 percent, but the recovery rate still can not meet the requirement, and the discharged water needs a special wastewater treatment system, so the method is not economical.
The energy-saving three-tower process adopts a mode of first-stage reduced pressure concentration, second-stage normal pressure concentration and third-stage reduced pressure rectification, is provided with a computer DCS control system, utilizes low-pressure steam as a heat source, can reduce the energy consumption of the system, has a DMF recovery rate of 93-95 percent, requires a special wastewater treatment system for discharged water, has odorous tail gas and cannot meet the current environmental protection requirement.
At present, colleges and enterprises research the geothermal heat pump rectification process, and the heat pump and the rectification tower are coupled to reduce energy consumption and improve the DMF recovery rate, but the technology is still not mature enough. The method mainly shows that micromolecular polyurethane and lignin in the wastewater cannot be well separated from the wastewater and enter a rectification system, so that a reboiler and a tower are seriously blocked, and the heat exchange effect is influenced; the whole device is seriously corroded due to inaccurate system design, equipment type selection and equipment material; the process is not complete enough, and the discharged water and tail gas cannot reach the standard, so that the environmental protection problem is caused; the whole device has a series of problems of high energy consumption and the like, so that the device cannot run for a long time.
Disclosure of Invention
Not enough to prior art, the utility model aims to provide a synthetic leather waste water treatment and DMF retrieve new technology, it is not high to solve current DMF rate of recovery, and outer drainage and tail gas are not up to standard, the problem that the energy consumption is high.
In order to achieve the above purpose, the utility model adopts the following technical means:
the system adopts four-stage negative pressure rectification and a mode of series connection of two-stage water vapor compressors for heat supply; preheating synthetic leather wastewater containing DMF, then feeding the synthetic leather wastewater into a vaporization tank, completely vaporizing the synthetic leather wastewater containing DMF in the vaporization tank, feeding the synthetic leather wastewater containing DMF into a first-stage dehydration tower in a gas-phase feeding manner for mass transfer separation, feeding the generated DMF, heavy component solution and formic acid into a second-stage rectification tower for mass transfer separation, conveying dimethylamine odor and the like formed by trace decomposition of the DMF in the second-stage rectification tower into water vapor, conveying the dimethylamine odor and the like out of the tower top of the second-stage rectification tower, pumping negative pressure by using a vacuum pump, taking condensed water vapor condensate as reflux liquid to flow back to the middle part of the dehydration tower, and conveying uncondensed gas of dimethylamine and the like to a tail gas treatment device. The DMF, the formic acid and the high-boiling residues at the bottom of the second-stage rectification tower enter a third-stage deacidification tower for mass transfer separation; the water vapor at the outlet of the first-stage water vapor compressor is used as a heat source for the vaporization tank; saturated steam at the outlet of the secondary steam compressor is used as a heat source of the deamination tower and the deacidification tower.
Further, a gas phase feed inlet is arranged in the middle of the first-stage dehydration tower, stainless steel pore plate corrugated packing is adopted above the gas phase feed inlet in the first-stage dehydration tower, the DMF, the heavy component solution and the formic acid are subjected to mass transfer separation with the top reflux liquid of the first-stage dehydration tower in the stainless steel pore plate corrugated packing, and the generated DMF and the heavy component solution fall into the bottom of the first-stage dehydration tower and circularly enter a reboiler of the dehydration tower; the heat source of the reboiler of the dehydration tower is derived from saturated steam at the outlet of the secondary steam compressor; the reflux ratio of the first-stage dehydration tower is 0.45-3, and the vacuum degree is 20-40 kpa.
Further, when the concentration of DMF at the top of the first-stage dehydration tower reaches more than 80%, the DMF enters the second-stage rectifying tower from the middle part of the second-stage rectifying tower for mass transfer separation, dimethylamine odor formed by the decomposition of DMF in the second-stage rectifying tower is entrained in water vapor and sent into the third-stage deamination tower from the top of the second-stage rectifying tower, DMF, a small amount of formic acid and heavy component solution fall back to the bottom of the second-stage rectifying tower and then sent into a reboiler of the rectifying tower, the heat source of the reboiler of the rectifying tower is saturated vapor from a second-stage water vapor compressor, and the concentration of DMF at the outlet of the second-stage; the reflux ratio of the second-stage rectifying tower is 0.6-3, and the vacuum degree of the top of the second-stage rectifying tower is 15-30 kpa.
Further, a feeding hole of the deacidification tower is formed in the middle of the third-stage deacidification tower, stainless steel hole plate corrugated packing is filled above the feeding hole of the deacidification tower in the third-stage deacidification tower, the material is S30408, the stainless steel hole plate corrugated packing is filled below the feeding hole of the deacidification tower, the material is S31603, DMF, formic acid and high-boiling-point substances enter from the feeding hole of the deacidification tower and are subjected to mass transfer separation with reflux liquid at the top of the third-stage deacidification tower, and the DMF falls back into a cavity at the top of the third-stage deacidification tower in a liquid state, wherein the concentration of the DMF reaches above 98.
And further, an interface for adding alkali liquor is arranged in the middle of the four-stage deamination tower, water vapor separated from the tops of the first-stage dehydration tower and the second-stage rectification tower is sent to the four-stage deamination tower, and the amount of sodium hydroxide is added according to the content of DMF in the water vapor.
Furthermore, an interface for adding acid liquor is arranged on the four-stage deamination tower at the same time for adjusting the pH value of external drainage water generated by the four-stage deamination tower.
Further, the temperature of the steam at the outlet of the first-stage steam compressor is 101-110 ℃; the temperature of the steam at the outlet of the secondary steam compressor is 115-130 ℃.
Further, the kettle residue in the synthetic leather wastewater containing DMF after vaporization is sent into a first kettle residue evaporation tank from the bottom of the vaporization tank, the kettle residue is reheated by using water vapor from an outlet of a second-stage water vapor compressor as a heat source, and water and DMF in the kettle residue are sent into a first-stage dehydration tower in a gaseous state again.
Further, residual kettle residues in the first kettle residue evaporation tank are conveyed into a second kettle residue evaporation tank from the bottom of the first kettle residue evaporation tank, raw steam is utilized for secondary evaporation, water and DMF in the residual kettle residues are conveyed into the primary dehydration tower in a gaseous state again, and final kettle residues generated by the second kettle residue evaporation tank are conveyed out from the bottom.
Compared with the prior art, the utility model discloses following profitable technological effect has:
the utility model provides a scheme that four tower negative pressure rectification and two-stage compressor establish ties and provide the heat source for whole rectification technology, ingenious adoption all gaseous phase feeding's mode provides the system solution for synthetic leather enterprise contains DMF complex composition waste water treatment and DMF recovery. The whole rectification system adopts negative pressure operation, reduces the temperature required by rectification, avoids DMF (boiling point: 153 ℃) from generating rapid hydrolysis due to high temperature, and the two-stage compressor series connection can accurately control the temperature of the whole rectification system, and avoids DMF large-scale decomposition caused by inaccurate temperature control.
By the system of the utility model, the DMF recovery rate can be improved by 3-5% on the basis of the prior art; so that the COD, ammonia nitrogen and total nitrogen of the external drainage water meet the national and local environmental protection requirements (the COD is less than or equal to 500 mg/m)3(ii) a Ammonia nitrogen is less than or equal to 35mg/m3(ii) a Total nitrogen is less than or equal to 70mg/m3) (ii) a The odor index of the tail gas emission is less than or equal to 2000 (the height of a chimney is 15 meters), and the VOCs is less than or equal to 200mg/m3(ii) a Compared with the prior art, the energy consumption of the system is reduced by more than 40%.
Drawings
Fig. 1 is a schematic diagram of the system of the present invention.
In the figure, 1, a heat exchanger; 2. a vaporization tank; 3. a vaporization tank reboiler; 4. a first still residue evaporation tank; 5. a first-stage dehydration tower; 6. a dehydration column reboiler; 7. a secondary rectification column; 8. a rectifying tower reboiler; 9. a third-stage deacidification tower; 10; a deacidification tower reboiler; 11. a four-stage deamination tower; 12. a reboiler of the deamination tower; 13. a first stage steam compressor; 14. a secondary water vapor compressor; 15. a second still residue evaporation tank; 16. a DMF heat exchanger; 17. DMF, water, light components cooler.
The embodiments of the present invention will be further described with reference to the drawings and examples.
Detailed Description
The utility model discloses cauldron residue in the synthetic leather waste water that contains DMF after the vaporization mainly refers to micromolecular polyurethane, lignin, cloth wadding, silt, trace DMF etc.. And the kettle residue is evaporated twice, so that DMF in the kettle residue is extracted and collected, and in addition, water is removed, the weight of the kettle residue is reduced, and the cost for treating the kettle residue is reduced.
The raw steam of the utility model is fresh saturated vapor, and the temperature is generally 160-fold and 190 ℃.
The negative pressure value of the second-stage rectifying tower is-20 to-35 kpa, the rectifying tower is pumped into the negative pressure mainly through the vapor compressor, and the steam does not need to provide heat for rectification, so that the energy consumption of the system is reduced.
The high-boiling-point substance at the bottom of the second-stage rectification tower mainly refers to an azeotrope formed by formic acid and water solution.
The reflux liquid at the top of the three-stage deacidification tower of the utility model is mainly DMF solution, and the temperature is 85-98 ℃.
The system of the utility model includes, first order dehydration tower, second grade rectifying column, tertiary deacidification tower and level four deamination tower are level four rectification technology, and the result principal ingredients that first order dehydration tower, second grade rectifying column produced are the same basically, are DMF, heavy ends solution and formic acid, and the difference is that the concentration of DMF all has the improvement after each level, has a gradient change 80%, 95% and 98%, and this is very difficult realization in the industry.
Example 1:
the embodiment provides a synthetic leather wastewater treatment and DMF recovery system, firstly DMF-containing wastewater (raw water) is discharged to reach the standard and is preheated by a heat exchanger 1 and then enters a vaporization tank 2, 101-110 ℃ water vapor at an outlet of a first-stage water vapor compressor 13 is used for providing a heat source for the vaporization tank 2, the vaporization tank 2 adopts negative pressure to completely vaporize the wastewater in the vaporization tank 2 and then enters a first-stage dehydration tower 5, namely a first rectifying tower, in a complete gas phase form. By adopting the scheme of all gas-phase feeding, the phenomenon that wastes such as a large amount of micromolecule polyurethane, lignin, cotton wadding and heavy components enter a system along with wastewater to cause the blockage of fillers in a reboiler and a tower and influence on the heat exchange efficiency and the rectification separation effect is avoided. The kettle residues (micromolecular polyurethane, lignin, cotton wool, sludge, trace DMF and the like) in the wastewater are gathered at the bottom of the vaporization tank 2, are pumped out by a sludge pump and are sent into a first kettle residue evaporation tank 4, the kettle residues are heated again by using steam at the outlet (115-125 ℃) of a secondary steam compressor 14 as a heat source, and the water and the DMF in the kettle residues are sent into a first-stage dehydration tower 5 (tower 1) in a gaseous state again. And then pumping out the kettle residue from the bottom of the first kettle residue evaporation tank 4 and sending the kettle residue into the second kettle residue evaporation tank 15, carrying out secondary evaporation by using raw steam (160-. And the kettle residue is evaporated twice, so that DMF in the kettle residue is extracted and collected, and in addition, water is removed, the weight of the kettle residue is reduced, and the cost for treating the kettle residue is reduced.
Gaseous water, DMF and trace heavy components enter a first-stage dehydration tower 5, stainless steel pore plate corrugated structured packing is adopted above a gas phase feed inlet, the water, the DMF and the heavy components are subjected to mass transfer separation with tower top reflux liquid in the packing, the water enters a water vapor compressor from the tower top in a gaseous form to increase the enthalpy value, and the first-stage rectification tower 5 is pumped into negative pressure (-20 to 35kpa) by using the water vapor compressor without providing heat for rectification by using raw steam, so that the energy consumption of the system is reduced. DMF and heavy components fall into the bottom of the tower after being separated from a large amount of water, circularly enter a reboiler 6 of a dehydration tower, and the heat source is from a secondary vapor compressor 14. When the concentration of DMF in the tower reaches more than 80 percent, the mixture enters a second-stage rectifying tower 7(2 towers). The reflux ratio of the first-stage dehydration tower 5 is 0.45-3, and the vacuum degree is 20-40 kpa. The whole rectifying device adopts negative pressure operation, reduces the system temperature, reduces the system energy consumption on one hand, can avoid DMF from accelerating decomposition due to high temperature on the other hand, improves the DMF recovery rate by 2-5% compared with the traditional scheme, and has the benefit of about 2000 ten thousand yuan which can be improved due to the improvement of the recovery rate every year according to the processing scale of a 50t/h device. (DMF concentration in wastewater is 20%, and DMF market price is 5000 yuan/ton).
DMF and heavy component solution with the concentration of more than 80 percent are sent out from the bottom of the first-stage dehydration tower 5 and enter the second-stage rectification tower 7 from the middle part, and the second-stage rectification tower 7 adopts stainless steel pore plate corrugated regular packing. The formic acid formed by decomposing the DMF, the heavy components and the DMF rises from the middle part of the tower, the reflux liquid at the top of the tower, the gaseous DMF and the heavy components are subjected to mass transfer separation in the filler, finally the water vapor is discharged from the top of the tower, and the DMF, a small amount of formic acid and the heavy components fall back to the bottom of the tower. Formic acid is concentrated in the three-stage deacidification tower 9 to be removed, the S31603 stainless steel material is adopted only in the equipment with high formic acid content in the three-stage deacidification tower 9, and the S30408 material can be selected as other materials, so that the equipment investment cost and the inspection and maintenance cost are reduced. Dimethylamine odor formed by the decomposition of DMF in the tower is entrained in water vapor and sent to a tail gas treatment system from the top of the tower. The heat source of the rectifying tower reboiler 8 is saturated vapor (115-130 ℃) from the secondary vapor compressor 14, the reflux ratio is 0.6-3, and the vacuum degree at the top of the tower is 15-30 kpa. The concentration of DMF reaches more than 95 percent. Two stages of vapor compressors are connected in series to provide heat for the whole process device, so that the temperature stability of all positions of the device is ensured. The temperature of the steam at the outlet of the first-stage steam compressor 13 is low (90-110 ℃) and is used for units with low system temperature requirements, and the temperature of the steam at the outlet of the second-stage steam compressor 14 is high (115-130 ℃) and is used for units with high system temperature requirements. The steam with different temperatures is reasonably matched and used in different reaction units, so that the consumption of raw steam can be reduced, and the production cost is reduced.
DMF, formic acid and high-boiling-point substances (an azeotrope formed by the formic acid and the aqueous solution) at the bottom of the second-stage rectifying tower 7 enter the middle part of a third-stage deacidification tower 9(3 towers), stainless steel pore plate corrugated structured packing is filled above a feed inlet of the deacidification tower and is made of S30408, and stainless steel pore plate corrugated structured packing is filled below the feed inlet and is made of S31603 (mainly because the formic acid concentration at the top of the tower is low, the corrosivity is not strong, the formic acid concentration at the bottom of the tower is high, and the corrosion is serious). DMF, formic acid and high-boiling residues enter the tower from the middle part of the tower, are subjected to mass transfer separation with reflux liquid (DMF solution at 85-98 ℃) at the top of the tower in a filler, and are returned to a cavity at the top of the deacidification tower in a liquid state (the concentration reaches more than 98%), pumped out of the system, cooled by a DMF heat exchanger 16 and stored. DMF, formic acid and high-boiling residues at the bottom of the tower enter a second kettle residue evaporation tank 15, are concentrated by using raw steam (170-190 ℃) and then are filled into a kettle residue barrel together for delivery. And a DMF, water and light component cooler 17 between the first-stage dehydration tower 5 and the second-stage rectification tower 7 further recovers heat for reuse.
The water vapor separated from the top of the first-stage dehydration tower 5 and the second-stage rectification tower 7 contains trace DMF and dimethylamine, and cannot be directly discharged, and the trace DMF and the dimethylamine in the water at the top of the tower need to be removed, so that the COD in the externally discharged water, the total nitrogen and the ammonia nitrogen can be discharged after reaching the standard. The utility model discloses an utilize the characteristic that DMF can decompose in a large number rapidly under alkaline environment, will contain the top water of trace DMF and dimethylamine and send into level four deamination tower 11(4 towers), utilize 14 exports (115 ℃ -130 ℃) of second grade vapor compressor saturated steam as the heat source to at level four deamination tower 11 middle part design interface of sodium hydroxide, according to the quantity that the top water DMF content decision added sodium hydroxide. After trace DMF is decomposed, dimethylamine and formic acid are formed, the formic acid reacts with sodium hydroxide to produce salts, and the salts are discharged out of the system, and an acid adding and blending interface is designed to adjust the pH value of external drainage water to reach the standard. And the non-condensable gas and dimethylamine odor generated by the dehydration tower reboiler 6, the rectification tower reboiler 8, the deacidification tower and the deamination tower are all treated by a tail gas treatment system. The formed dimethylamine sulfate solution can form dimethylamine sulfate products for the chemical industry after concentration. This tail gas processing system does the utility model discloses the public utility model of people's earlier stage does not do the detailed introduction here.
The utility model discloses some units have been verified on Zhejiang shan drum energy development limited company's synthetic leather waste water centralized control and DMF recovery first-term project of Zhejiang lishu investment construction, and whole device adopts two-stage vapor compressor to establish ties and negative pressure operation, compares with three traditional towers and three energy-saving towers, can reduce energy consumption 45% -50%. (the original energy-saving three towers need 0.68 ton steam and 20 degrees electricity for treating one ton of wastewater, the total energy cost is 151 yuan/ton of wastewater; the utility model has the advantages of 102 degrees for treating one ton of water, 0.03 ton of raw steam, and 82.5 yuan for treating one ton of wastewater). The whole set of device controls the index of the water discharged from the top of the tower to be less than or equal to 500mg/m3And ammonia nitrogen is less than or equal to 35mg/m3Total nitrogen is less than or equal to 70mg/m3The odor index of the discharged exhaust gas is controlled within 2000 (dimensionless), and the VOCs is controlled at 200mg/m3. The second-phase construction is carried out according to the whole scheme, and the Yuanyue can be put into operation in 2021.
Claims (9)
1. The synthetic leather wastewater treatment and DMF recovery system is characterized by comprising a vaporization tank, a first-stage dehydration tower, a second-stage rectification tower, a third-stage deacidification tower, a fourth-stage deamination tower, a first-stage vapor compressor and a second-stage vapor compressor which are connected in parallel, wherein the vapor at the outlet of the first-stage vapor compressor is used as a heat source for the vaporization tank; saturated steam at the outlet of the second-stage water vapor compressor is used as a heat source of a dehydration tower, a DMF refining tower, a deamination tower and an deacidification tower;
preheating synthetic leather wastewater containing DMF, then feeding the synthetic leather wastewater into a vaporization tank, completely vaporizing the synthetic leather wastewater containing DMF in the vaporization tank, so that the synthetic leather wastewater containing DMF enters a first-stage dehydration tower in a gas-phase feeding manner for mass transfer separation, the generated DMF, heavy component solution and formic acid enter a second-stage rectification tower for mass transfer separation, dimethylamine odor generated by trace decomposition of DMF in the second-stage rectification tower is carried in water vapor and is sent out from the top of the second-stage rectification tower, condensed water vapor condensate serving as reflux liquid flows back to the middle part of the dehydration tower, dimethylamine noncondensable gas is sent to a tail gas treatment device, and DMF, formic acid and high-boiling substances at the bottom of the second-stage rectification tower enter a third-stage deacidification tower for mass transfer separation; wherein, the water vapor at the outlet of the first stage water vapor compressor is used as a heat source provided by the vaporization tank.
2. The synthetic leather wastewater treatment and DMF recovery system of claim 1, wherein a gas phase feed port is arranged in the middle of the first-stage dehydration tower, stainless steel perforated plate corrugated packing is adopted above the gas phase feed port in the first-stage dehydration tower, DMF, heavy component solution and formic acid are subjected to mass transfer separation with the top reflux liquid of the first-stage dehydration tower in the stainless steel perforated plate corrugated packing, and the generated DMF and heavy component solution fall into the bottom of the first-stage dehydration tower and circularly enter a reboiler of the dehydration tower; the heat source of the reboiler of the dehydration tower is derived from saturated steam at the outlet of the secondary steam compressor; the reflux ratio of the first-stage dehydration tower is 0.45-3, and the vacuum degree is 20-40 kpa.
3. The synthetic leather wastewater treatment and DMF recovery system of claim 1, wherein DMF at the bottom of the primary dehydration tower enters from the middle part of the secondary rectification tower for mass transfer separation when the concentration of DMF reaches more than 80%, DMF in the secondary rectification tower has dimethylamine odor formed by micro decomposition entrained in water vapor and is discharged from the top of the secondary rectification tower, vacuum pump is used for pumping negative pressure, condensed water vapor condensate is taken as reflux liquid and flows back to the middle part of the dehydration tower, and dimethylamine is not condensed and is sent to the tail gas treatment device; the DMF, a small amount of formic acid and heavy component solution fall back to the bottom of the secondary rectifying tower and then are sent into a reboiler of the rectifying tower, the heat source of the reboiler of the rectifying tower is from saturated steam of a secondary steam compressor, and the concentration of the DMF at the outlet of the secondary rectifying tower reaches more than 95 percent; the reflux ratio of the second-stage rectifying tower is 0.6-3, and the vacuum degree of the top of the second-stage rectifying tower is 15-30 kpa.
4. The synthetic leather wastewater treatment and DMF recovery system of claim 1, wherein the middle part of the third-stage deacidification tower is provided with a deacidification tower feed inlet, stainless steel pore plate corrugated filler is filled above the deacidification tower feed inlet in the third-stage deacidification tower, the material is S30408, the stainless steel pore plate corrugated filler is filled below the deacidification tower feed inlet, the material is S31603, DMF, formic acid and high-boiling substances enter from the deacidification tower feed inlet and perform mass transfer separation with the tower top reflux liquid of the third-stage deacidification tower, and DMF falls back into the top cavity of the third-stage deacidification tower in a liquid state, and the concentration of DMF reaches more than 98 percent at the moment.
5. The synthetic leather wastewater treatment and DMF recycling system of claim 1, wherein the middle part of the four-stage deamination tower is provided with an interface for adding alkali liquor, the water vapor separated from the top of the first-stage dehydration tower and the second-stage rectification tower is sent to the four-stage deamination tower, and the amount of sodium hydroxide is added according to the content of DMF in the water vapor.
6. The synthetic leather wastewater treatment and DMF recycling system of claim 5, wherein an acid adding port is arranged on the four-stage deamination tower at the same time for adjusting the pH value of external drainage water generated by the four-stage deamination tower.
7. The synthetic leather wastewater treatment and DMF recovery system of claim 1, wherein the temperature of the water vapor at the outlet of the primary water vapor compressor is 101 ℃ to 110 ℃; the temperature of the steam at the outlet of the secondary steam compressor is 115-130 ℃.
8. The synthetic leather wastewater treatment and DMF recycling system of claim 1, wherein the still residue in the synthetic leather wastewater containing DMF after vaporization is sent into a first still residue evaporation tank from the bottom of the vaporization tank, the still residue is heated again by using the water vapor from the outlet of the second stage water vapor compressor as a heat source, and the water and DMF in the still residue are sent into the first stage dehydration tower again in gaseous form.
9. The synthetic leather wastewater treatment and DMF recycling system of claim 8, wherein the residual kettle residue in the first kettle residue evaporating pot is sent into the second kettle residue evaporating pot from the bottom of the first kettle residue evaporating pot, secondary evaporation is carried out by using raw steam, the water content and DMF in the residual kettle residue are sent into the first-stage dehydration tower again in a gaseous state, and the final kettle residue generated by the second kettle residue evaporating pot is sent out from the bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021721446.0U CN212864613U (en) | 2020-08-17 | 2020-08-17 | Synthetic leather waste water treatment and DMF recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021721446.0U CN212864613U (en) | 2020-08-17 | 2020-08-17 | Synthetic leather waste water treatment and DMF recovery system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212864613U true CN212864613U (en) | 2021-04-02 |
Family
ID=75221842
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021721446.0U Active CN212864613U (en) | 2020-08-17 | 2020-08-17 | Synthetic leather waste water treatment and DMF recovery system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212864613U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111943865A (en) * | 2020-08-17 | 2020-11-17 | 西安联创分布式可再生能源研究院有限公司 | Synthetic leather waste water treatment and DMF recovery system |
| CN114057340A (en) * | 2021-11-10 | 2022-02-18 | 浙江闽锋化学有限公司 | Novel DMF (dimethyl formamide) recovery device and using method thereof |
| CN115382238A (en) * | 2022-08-24 | 2022-11-25 | 吉安巨联环保科技有限公司 | Method for reducing energy consumption of DMF waste liquid comprehensive utilization equipment |
| CN117883803A (en) * | 2024-03-18 | 2024-04-16 | 宁波新溶聚企业管理合伙企业(有限合伙) | Solvent rectification heat energy utilization device and method integrating heat pump rectification and triple-effect rectification |
-
2020
- 2020-08-17 CN CN202021721446.0U patent/CN212864613U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111943865A (en) * | 2020-08-17 | 2020-11-17 | 西安联创分布式可再生能源研究院有限公司 | Synthetic leather waste water treatment and DMF recovery system |
| CN114057340A (en) * | 2021-11-10 | 2022-02-18 | 浙江闽锋化学有限公司 | Novel DMF (dimethyl formamide) recovery device and using method thereof |
| CN114057340B (en) * | 2021-11-10 | 2024-03-19 | 浙江闽锋化学有限公司 | Use method of DMF recovery device |
| CN115382238A (en) * | 2022-08-24 | 2022-11-25 | 吉安巨联环保科技有限公司 | Method for reducing energy consumption of DMF waste liquid comprehensive utilization equipment |
| CN117883803A (en) * | 2024-03-18 | 2024-04-16 | 宁波新溶聚企业管理合伙企业(有限合伙) | Solvent rectification heat energy utilization device and method integrating heat pump rectification and triple-effect rectification |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN212864613U (en) | Synthetic leather waste water treatment and DMF recovery system | |
| CN111943865A (en) | Synthetic leather waste water treatment and DMF recovery system | |
| CN111302899B (en) | Ammonia and tertiary butanol recovery device and method in cyclohexanone ammoximation production process | |
| CN104788289A (en) | Heat pump coupling process for ethylene glycol rectification | |
| CN111392947B (en) | Ammonia water resource utilization process and device | |
| CN105967425A (en) | Coal chemical industry grey water flashing treatment system capable of reducing ammonia accumulation and coal chemical industry grey water flashing treatment process capable of reducing ammonia accumulation | |
| CN104817481A (en) | Technological method for recovering DMSO from DMSO aqueous solution | |
| CN103830921A (en) | System and technology for evaporation concentration of extraction water | |
| CN106964174B (en) | Method and system for rectifying/purifying ammonia | |
| CN205269079U (en) | Energy -conserving environmental protection system of multiple effect evaporation alkali recovery | |
| CN204661587U (en) | A kind of energy-saving carbamide production system | |
| CN212222702U (en) | High-efficient low temperature negative pressure ammonia nitrogen waste water strip system | |
| CN113813623A (en) | MVR concentration and rectification system and recovery method of DMAC waste liquid | |
| CN212050954U (en) | Ammonia water resource utilization device | |
| CN210214856U (en) | Energy-efficient surplus aqueous ammonia distillation plant | |
| CN201686513U (en) | Steam afterheat utilization unit and system for vacuum device of sea water desalination system | |
| CN110902742A (en) | Method for recovering organic matters in high-concentration organic wastewater | |
| CN212482152U (en) | Waste water treatment system of crude phenol extraction technology | |
| CN114409004A (en) | Energy-saving recycling process for treating wastewater containing volatile substances | |
| CN208200783U (en) | A kind of alkyl esterification method glyphosate solvent recovering system based on three-level condensation | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN217921534U (en) | Ammonia water recovery system | |
| CN208747971U (en) | A kind of alkyl esterification method production glyphosate solvent recovering system based on B-grade condensation | |
| CN218620397U (en) | DMF waste water recovery system device | |
| CN220317460U (en) | Energy-saving deamination and ammonia water recovery device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |