CN111186870A - Device for efficiently treating ammonia nitrogen problem of high-salinity organic wastewater - Google Patents
Device for efficiently treating ammonia nitrogen problem of high-salinity organic wastewater Download PDFInfo
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- CN111186870A CN111186870A CN202010137121.6A CN202010137121A CN111186870A CN 111186870 A CN111186870 A CN 111186870A CN 202010137121 A CN202010137121 A CN 202010137121A CN 111186870 A CN111186870 A CN 111186870A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 44
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 27
- 239000012452 mother liquor Substances 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- 230000009615 deamination Effects 0.000 claims description 17
- 238000006481 deamination reaction Methods 0.000 claims description 17
- 239000007791 liquid phase Substances 0.000 claims description 14
- 238000004821 distillation Methods 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 11
- 239000000498 cooling water Substances 0.000 claims description 6
- 239000010815 organic waste Substances 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 150000003839 salts Chemical class 0.000 claims description 5
- 239000003507 refrigerant Substances 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 4
- 238000009835 boiling Methods 0.000 abstract description 3
- 238000001704 evaporation Methods 0.000 abstract description 2
- 230000008020 evaporation Effects 0.000 abstract description 2
- 239000002440 industrial waste Substances 0.000 abstract description 2
- 238000005187 foaming Methods 0.000 abstract 1
- 239000000463 material Substances 0.000 description 15
- 238000009833 condensation Methods 0.000 description 10
- 230000005494 condensation Effects 0.000 description 10
- 239000007789 gas Substances 0.000 description 9
- 238000005265 energy consumption Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 239000013589 supplement Substances 0.000 description 7
- 230000010354 integration Effects 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000002243 precursor Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F1/06—Flash 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a device for efficiently treating ammonia nitrogen in high-salinity organic wastewater, and belongs to the technical field of industrial waste treatment equipment. The method comprises the following steps: the heat exchanger is communicated with the side wall of the rectifying tower, the top of the rectifying tower is communicated with the tower top condenser, the tower top condenser is communicated with a first plate at the top of the rectifying tower through a gas-liquid separation tank, the lower end of the rectifying tower is provided with a rectifying tower kettle, the bottom of the rectifying tower kettle is communicated with a reboiler, the top of the reboiler is communicated with the rectifying tower kettle, the bottom of the reboiler is communicated with a condensate flash tank, and steam generated by the condensate flash tank is conveyed back to the rectifying tower kettle. The device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater provided by the invention solves the problems of easiness in foaming, high boiling point rise and the like in direct evaporation, and simultaneously reduces the system operation cost.
Description
Technical Field
The invention relates to the technical field of industrial waste treatment equipment, in particular to a device for efficiently treating ammonia nitrogen in high-salinity organic wastewater.
Background
At present, ammonia nitrogen treatment in high-salt organic wastewater is always an urgent problem to be solved in the industry, and conventional treatment modes comprise an electrolysis method, a stripping tower, a rectifying tower and the like. Wherein, the recovery rate of products at the top of the tower and the content of ammonia nitrogen in the water discharged from the bottom of the tower are main performance indexes in the operation process of the system. And the rectification debugging mainly depends on controlling the reflux of the tower top to realize the purity requirement of the tower top product. The problem of high energy consumption of the system is caused by large reflux quantity, and the reasonable utilization of the energy is particularly important.
Disclosure of Invention
Aiming at the problems in the prior art, the device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater is provided, the device realizes the integration of the energy related to the system to the maximum degree on the basis of meeting the product purity of the tower top and the tower kettle, and can greatly reduce the energy consumption brought by the operation process of the system.
The specific technical scheme is as follows:
the utility model provides a device of high-efficient processing high salt organic waste water ammonia nitrogen problem mainly includes: the system comprises a rectifying tower, a rectifying tower kettle, a heat exchanger, a tower top condenser, a reboiler and a condensate flash tank.
Mother liquor wastewater (namely organic wastewater containing ammonia nitrogen) and deamination effluent flow through the heat exchanger, wherein the mother liquor wastewater and the deamination effluent are separated from each other, the temperature of the mother liquor wastewater is low, the temperature of the deamination effluent is high, the mother liquor wastewater and the deamination effluent perform countercurrent heat exchange inside the heat exchanger, and the mother liquor wastewater is promoted to be heated to a bubble point (a critical point of the temperature for separating a first batch of bubbles from a liquid phase) in the heat exchanger.
Mother liquor wastewater flows into the rectifying tower after flowing through the heat exchanger, gas and liquid phases in the rectifying tower form the same tower plate, the rectifying tower adopts a reboiler form, and the reboiler form is defaulted to be one tower plate.
One end of the tower top condenser is communicated with the top of the rectifying tower, light components (low-boiling-point substances) in a liquid phase are output from the tower top, then, light component steam at the tower top enters the tower top condenser to be primarily condensed, the other end of the tower top condenser is communicated with the second-stage condenser, the other end of the tower top condenser is communicated with the gas-liquid separation tank, the gas-liquid separation tank is communicated with a first tower plate at the tower top of the rectifying tower, partial material discharged by the tower top condenser after condensation is discharged into the subsequent second-stage condenser, secondary condensation is carried out, and partial material is separated by the gas-liquid separation tank and then flows back to the first plate at the tower top.
The rectifying tower kettle is arranged at the lower end of the rectifying tower and communicated with the rectifying tower, heavy components in a liquid phase in the rectifying tower finally flow into the rectifying tower kettle, and deamination effluent at the bottom of the rectifying tower kettle is conveyed into the heat exchanger and then discharged to the outside.
The bottom of the rectifying tower kettle is also communicated with the bottom of the reboiler, and the top of the reboiler is communicated with one side of the rectifying tower kettle.
One side of reboiler and the lateral wall intercommunication of condensate flash tank, the top of condensate flash tank and the steam input port intercommunication of rectifying column tower cauldron, the department intercommunication is collected with the comdenstion water to the bottom of condensate flash tank, and the condensate flash tank carries out the secondary separation with steam condensate, and in hot steam got into the rectifying column tower cauldron, the comdenstion water was discharged to the foreign world from the bottom of condensate flash tank.
In the device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater, the device is also characterized in that one side of the tower top condenser is provided with a circulating cooling water supply pipe and a circulating cooling water return pipe, and the refrigerant of the tower top condenser is frozen water.
In the device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater, the device is also characterized in that the top of the gas-liquid separation tank is communicated with a secondary condenser.
In the device of foretell high salt organic waste water ammonia nitrogen problem of high efficiency processing, still have such characteristic, still include the bright steam source, the bright steam of part of bright steam source output is the heat medium of reboiler, bright steam source and reboiler intercommunication.
In the device for efficiently treating the ammonia nitrogen problem of the high-salt organic wastewater, the device is further characterized in that part of fresh steam output by the fresh steam source is communicated with a steam input port of a tower kettle of the rectifying tower.
In the foretell device of high salt organic waste water ammonia nitrogen problem, still have such characteristic, be provided with first valve between bright steam source and the reboiler, be provided with the second valve between bright steam source and the distillation column tower cauldron, be provided with the third valve between condensate flash tank and the distillation column tower cauldron.
In the device for efficiently treating the ammonia nitrogen problem of the high-salt organic wastewater, the device is also characterized in that a reflux pump is arranged between the gas-liquid separation tank and the rectifying tower.
In the device for efficiently treating the ammonia nitrogen problem of the high-salt organic wastewater, the device is also characterized in that a tower kettle discharge pump is arranged between the rectifying tower kettle and the heat exchanger.
The positive effects of the technical scheme are as follows:
the invention provides a device for efficiently treating ammonia nitrogen in high-salinity organic wastewater,
1. materials (deamination effluent) in the tower kettle of the rectifying tower and the mother liquor wastewater are subjected to countercurrent heat exchange in the heat exchanger, so that energy integration is realized, and the utilization efficiency of energy is improved.
2. This deamination device adopts partial condensation to satisfy the product purity at the rectifying column top of the tower, simultaneously can effective control reflux ratio, reduce system operation energy consumption, increase the operability and the adjustability of system operation.
3. Condensate generated after fresh steam is subjected to heat exchange in the reboiler enters the condensate flash tank, the steam is subjected to flash separation in the condensate flash tank, and separated gas phase enters the tower kettle of the rectifying tower for secondary utilization, so that energy integration is realized, and the thermodynamic efficiency of the system is improved.
4. A fresh steam input port is reserved in the rectifying tower, two modes of steam stripping and reboiler heating are effectively switched by switching of a steam valve, and separation of materials by multiple modes is achieved, so that the utilization efficiency of energy is improved.
Drawings
FIG. 1 is a system schematic diagram of an embodiment of the device for efficiently treating ammonia nitrogen in high-salinity organic wastewater.
In the drawings: 1. a heat exchanger; 2. a rectifying tower kettle; 3. a discharge pump of the tower kettle; 4. a rectifying tower; 5. a reboiler; 6. a tower top condenser; 7. a gas-liquid separation tank; 8. a reflux pump; 9. condensate flash tank; 10. a first valve; 11. a second valve; 12. a third valve.
A: fresh steam; b: water is discharged after deamination; c: mother liquor wastewater; d: a secondary condenser; e: and (5) condensing the steam.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the following embodiment specifically explains the device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater provided by the invention with reference to the attached drawing 1.
In this device of high-efficient processing high salt organic waste water ammonia nitrogen problem, it has mother liquor waste water C (containing the organic waste water of ammonia nitrogen promptly) and deamination play water B to flow through in heat exchanger 1, wherein mother liquor waste water C and deamination play water B separate each other, mother liquor waste water C's temperature is lower, deamination goes out water B's temperature higher, both carry out heat-transfer against current in heat exchanger 1 is inside, and make mother liquor waste water C heat to the bubble point (the critical point of the temperature of separating out first batch bubble from the liquid phase) in heat exchanger 1, this heat exchanger 1 has adopted high-efficient heat integration principle, the high-efficient utilization of heat integration has been realized.
Mother liquor waste water C flows through heat exchanger 1 and then flows into rectifying column 4 gas-liquid phase and constitutes the same column plate, and rectifying column 4 adopts reboiler 5's form, and this kind of reboiler 5 form is as a column plate, utilizes the reducible circulating water yield in the rectifying column of reboiler form, and reboiler 5 also is equivalent to a theoretical plate, can improve gas-liquid separation efficiency, reduces the whole energy consumption of system.
One end of the tower top condenser 6 is communicated with the top of the rectifying tower 4, light components (low-boiling-point substances) in a liquid phase are output from the tower top, then light component steam at the tower top enters the tower top condenser 6 to be primarily condensed, the other end of the tower top condenser 6 is communicated with the second-stage condenser D, the other end of the tower top condenser 6 is communicated with the gas-liquid separation tank 7, the gas-liquid separation tank 7 is communicated with a first tower plate at the tower top of the rectifying tower 4, partial material after condensation of the tower top condenser 6 is discharged to the subsequent second-stage condenser D to be secondarily condensed, and partial material is separated by the gas-liquid separation tank 7 and then flows back to the first plate at the tower top of the rectifying tower 4. The top condenser 6 realizes partial condensation and partial discharge of light components at the top of the rectifying tower 4, and the deamination system adopts a partial condensation form, so that the product purity at the top of the tower can be met, the reflux ratio can be effectively controlled, the system operation energy consumption is reduced, and the system operation operability is improved.
The rectifying tower kettle 2 is arranged at the lower end of the rectifying tower 4 and is communicated with the rectifying tower 4, heavy components in a liquid phase in the rectifying tower 4 finally flow into the rectifying tower kettle 2, deamination effluent at the bottom of the rectifying tower kettle 2 is conveyed into the heat exchanger 1 and then is discharged to the outside.
The bottom of the rectifying tower kettle 2 is also communicated with the bottom of a reboiler 5, and the top of the reboiler 5 is communicated with one side of the rectifying tower kettle 2. The reboiler 5 can realize material separation, and in the liquid phase entering condensate flash drum 9 in the reboiler 5, the gaseous phase in reboiler 5 continued to enter rectifying column tower 2.
Reboiler 5's one side and condensate flash tank 9's lateral wall intercommunication, condensate flash tank 9's top and rectifying column tower cauldron 2's steam input port intercommunication, condensate flash tank 9's bottom and comdenstion water are collected and are located the intercommunication, condensate flash tank 9 carries out the secondary separation with steam condensate water E, the reutilization in hot steam gets into rectifying column tower cauldron 2, realize energy integration, increase system thermodynamic efficiency, steam condensate water E is discharged to the outer from condensate flash tank 9's bottom.
In a preferred embodiment, as shown in fig. 1, a circulating cooling water supply pipe (CWS) and a circulating cooling water return pipe (CWR) are provided at one side of the overhead condenser 6, and the refrigerant of the overhead condenser 6 is frozen water, and the frozen water circulates and flows into the overhead condenser 6, so that organic matter with a low boiling point can be efficiently cooled, and the effect of condensing light components at the top of the tower can be ensured.
In a preferred embodiment, as shown in fig. 1, the top of the gas-liquid separation tank 7 is also communicated with the secondary condenser D, the gas phase in the gas-liquid separation tank 7 and the gas phase discharge of the tower top condenser 6 are merged into the secondary condenser D for secondary condensation, and the deamination system adopts a partial condensation form to meet the purity of a tower top product, effectively control the reflux ratio, and increase the operability of system operation while reducing the energy consumption of system operation.
In a preferred embodiment, as shown in fig. 1, the system further comprises a fresh steam source, part of the fresh steam a output by the fresh steam source is a heating medium of the reboiler 5, the fresh steam source is communicated with the reboiler 5, the amount of circulating water in the rectifying tower 4 can be reduced by using the form of the reboiler 5, and the reboiler 5 can be regarded as a tower plate, so that the gas-liquid separation efficiency of the system is improved, and the overall energy consumption of the system is reduced.
In a preferred embodiment, as shown in fig. 1, a part of the fresh steam a output by the fresh steam source is communicated with a steam input port of the rectifying tower kettle 2, and the steam input port is reserved at the rectifying tower kettle 2, so that the two modes of the reboiler 5 and the steam stripping are switched, and the stability of the system is increased.
In a preferred embodiment, as shown in fig. 1, a first valve 10 is provided between the fresh steam source and the reboiler 5, a second valve 11 is provided between the fresh steam source and the distillation column bottom 2, and a third valve 12 is provided between the condensate flash tank 9 and the distillation column bottom 2.
The mode that steam enters the rectifying tower 4 is adjusted through opening and closing of the first valve 10 and the second valve 11, the first valve 10 is opened, the second valve 11 is closed, and steam obtained through flash separation of the condensate flash tank 9 is used for supplementing the steam to the rectifying tower 4; when the first valve 10 is closed and the second valve 11 is opened, the steam supplement to the rectifying tower 4 is realized through the external fresh steam supplement; the first valve 10 and the second valve 11 are opened simultaneously, so that steam supplement to the rectifying tower 4 is realized simultaneously through the steam of the two steam sources, and the overall operation stability of the system can be improved through the reserved steam input port of the rectifying tower kettle 2 and a plurality of steam supplement modes.
In addition, the heating modes of the reboiler 5 and the rectifying tower 4 can be switched by opening and closing the second valve 11 and the third valve 12, and the material separation is realized by the reboiler 5 when the second valve 11 is closed and the third valve 12 is opened; when the second valve 11 is opened and the third valve 12 is closed, the system directly performs material separation in a steam stripping mode.
In a preferred embodiment, as shown in fig. 1, a reflux pump 8 is provided between the gas-liquid separation tank 7 and the rectifying tower 4, and the liquid phase in the gas-liquid separation tank 7 is returned to the top of the rectifying tower 4 by the reflux pump 8.
In a preferred embodiment, as shown in fig. 1, a column bottom discharge pump 3 is provided between the distillation column bottom 2 and the heat exchanger 1, and the column bottom liquid in the distillation column bottom 2 is transferred to the heat exchanger 1 by the column bottom discharge pump 3 to perform heat exchange.
Two specific embodiments are described below, and it should be noted that the structures, processes, and materials described in the following embodiments are only used to illustrate the feasibility of the embodiments, and are not intended to limit the scope of the present invention.
The device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater can solve the problems that the COD (Chemical Oxygen Demand) of the mother liquor wastewater in the ternary precursor production is high, the direct evaporation is easy to foam, the boiling point rise is high and the like, and simultaneously reduces the system operation cost.
After the ternary precursor mother liquor wastewater with high ammonia nitrogen content to be treated is preheated to a bubble point (a critical point of the temperature for separating a first batch of bubbles from a liquid phase) by a heat exchanger, the ternary precursor mother liquor wastewater enters a rectifying tower, gas and liquid phases form the same tower plate, the material entering a tower body of the rectifying tower is in countercurrent contact with the gas phase on the tower plate, multiple separation is realized, light components are output from the top of the tower, and light component steam at the top of the tower enters a condenser at the top of the tower for primary condensation. And a material part condensed by the tower top condenser is discharged to a subsequent secondary condenser, the other part of the material part is separated by the gas-liquid separation tank, a liquid phase flows back to the first tower plate at the top of the tower in the rectifying tower through the reflux pump, and a gas phase separated by the gas-liquid separation tank and a gas phase of the tower top condenser are converged and jointly enter the secondary condenser for secondary condensation. The refrigerant of the tower top condenser is preferably chilled water.
Condensate water generated after high-pressure fresh steam exchanges heat with kettle liquid in a tower kettle of the rectifying tower through a reboiler enters a condensate flash tank through a shell pass to perform secondary gas-liquid separation, condensate is discharged to the outside, steam generated secondarily enters the rectifying tower, and the amount of the steam entering the rectifying tower is adjusted through opening and closing of a first valve and a second valve. Wherein, the gas phase enters the rectifying tower to continuously carry out layer-by-layer tower plate gas-liquid separation after the kettle liquid in the rectifying tower exchanges heat through a reboiler.
The first valve is opened, the second valve is closed, then the steam supplement to the rectifying tower is realized only through the condensate separating tank, the first valve is closed, the second valve is opened, then the steam supplement to the rectifying tower is supplemented through external fresh steam, and the first valve and the second valve are opened simultaneously, then the steam supplement to the rectifying tower is supplemented through two steam sources simultaneously. In addition, the heating modes of the reboiler and the rectifying tower can be switched by opening and closing the second valve and the third valve, when the second valve is closed and the third valve is opened, the system realizes material separation through the reboiler, and when the first valve is opened and the second valve is closed, the system carries out material separation through direct steam stripping.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.
Claims (8)
1. The utility model provides a device of high-efficient processing high salt organic waste water ammonia nitrogen problem which characterized in that includes:
the heat exchanger is internally provided with mother liquor wastewater and deamination effluent in a flowing manner, wherein the mother liquor wastewater and the deamination effluent are mutually separated, and the mother liquor wastewater is heated to a bubble point in the heat exchanger;
the mother liquor wastewater flows into the rectifying tower after flowing through the heat exchanger, and the gas-liquid phase composition in the rectifying tower is the same;
the tower top condenser is communicated with the top of the rectifying tower at one end, the second-stage condenser at the other end and a gas-liquid separation tank at the other end, and the gas-liquid separation tank is communicated with a first tower plate at the top of the rectifying tower;
the distillation tower kettle is arranged at the lower end of the distillation tower and is communicated with the distillation tower, and deamination effluent at the bottom of the distillation tower kettle is conveyed into the heat exchanger;
the bottom of the rectifying tower kettle is also communicated with the bottom of the reboiler, and the top of the reboiler is communicated with one side of the rectifying tower kettle;
the condensate flash tank, one side of reboiler with the lateral wall intercommunication of condensate flash tank, the top of condensate flash tank with the steam input port intercommunication of rectifying column tower cauldron, the bottom and the comdenstion water of condensate flash tank are collected the department and are communicate.
2. The device for efficiently treating the ammonia nitrogen problem in the high-salinity organic wastewater as claimed in claim 1, wherein one side of the tower top condenser is provided with a recirculated cooling water supply pipe and a recirculated cooling water return pipe, and the refrigerant of the tower top condenser is frozen water.
3. The device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater according to claim 1, characterized in that the top of the gas-liquid separation tank is also communicated with the secondary condenser.
4. The device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater according to claim 1, further comprising a fresh steam source, wherein part of the fresh steam output by the fresh steam source is a heating medium of the reboiler, and the fresh steam source is communicated with the reboiler.
5. The device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater according to claim 4, wherein part of the fresh steam output by the fresh steam source is communicated with a steam input port of the tower kettle of the rectifying tower.
6. The device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater according to claim 5, wherein a first valve is arranged between the fresh steam source and the reboiler, a second valve is arranged between the fresh steam source and the distillation tower kettle, and a third valve is arranged between the condensate flash tank and the distillation tower kettle.
7. The device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater according to claim 1, characterized in that a reflux pump is arranged between the gas-liquid separation tank and the rectifying tower.
8. The device for efficiently treating the ammonia nitrogen problem of the high-salinity organic wastewater according to claim 1, characterized in that a tower kettle discharge pump is arranged between the rectifying tower kettle and the heat exchanger.
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| CN202010137121.6A CN111186870A (en) | 2020-03-02 | 2020-03-02 | Device for efficiently treating ammonia nitrogen problem of high-salinity organic wastewater |
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| CN202010137121.6A CN111186870A (en) | 2020-03-02 | 2020-03-02 | Device for efficiently treating ammonia nitrogen problem of high-salinity organic wastewater |
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| CN111569455A (en) * | 2020-05-26 | 2020-08-25 | 昆山三一环保科技有限公司 | Deamination tower system for recovering TVR (transient voltage suppressor) condensate and deamination method |
| CN112479296A (en) * | 2020-12-14 | 2021-03-12 | 昆山三一环保科技有限公司 | Deamination processing system |
| CN112759015A (en) * | 2020-12-31 | 2021-05-07 | 内蒙古蒙维科技有限公司 | Industrial wastewater recycling device and method for chemical industry |
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| CN208911492U (en) * | 2018-08-21 | 2019-05-31 | 天津辰力工程设计有限公司 | A kind of kettle material purification system again |
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