CN217757159U - High-salt organic wastewater evaporation device - Google Patents
High-salt organic wastewater evaporation device Download PDFInfo
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- CN217757159U CN217757159U CN202220977427.7U CN202220977427U CN217757159U CN 217757159 U CN217757159 U CN 217757159U CN 202220977427 U CN202220977427 U CN 202220977427U CN 217757159 U CN217757159 U CN 217757159U
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Abstract
The utility model provides a high salt organic waste water evaporation plant. High salt organic waste water gets into in the high temperature evaporation equipment, then let in high temperature flue gas in the combustion chamber in the high temperature evaporation equipment liquid, the tympanic bulla then and go out, take out liquid vapor, get into the blast pipe above the high temperature evaporation equipment, be equipped with the knockout tower in the blast pipe, the flue gas gets into the heat exchanger behind the knockout tower, carry out the heat transfer with the high salt organic waste water in the low temperature evaporation equipment, then, low temperature flue gas after the heat transfer mixes with the exhaust of low temperature evaporation equipment, the gas mixture carries out the heat transfer with the air that gets into the low temperature evaporation equipment, the air discharge after the heating goes into the low temperature evaporation equipment, carry out the low temperature evaporation, high salt organic waste water is after the preliminary treatment of low temperature evaporation equipment, discharge through the leakage fluid dram, get into high temperature evaporation equipment once more and handle. The process can fully utilize the waste heat of direct contact evaporation, reduce the energy consumption of the system and reduce the running cost of the system.
Description
Technical Field
The utility model relates to a sewage treatment field, concretely relates to high salt organic waste water evaporation plant.
Background
The main sources of the high-salt organic wastewater are production processes such as petrochemical industry, coal chemical industry, medicine, printing and dyeing and other wastewater treatment processes such as Electrodialysis (ED), nanofiltration membrane (NF), reverse Osmosis (RO) and the like. Such waste waters also contain a significant amount of inorganic ions in free form and, in addition, often contain a significant amount of organic components. And because the sources are different, the components of various high-salt organic wastewater are complex and changeable, the working condition change of the treatment process is increased, and the treatment difficulty of the wastewater is increased.
At present, the treatment method of high-salt organic wastewater mainly comprises a membrane method, a thermal method and a coupling technology. The most critical of the membrane process is the cost of its industrial production, and the frequent replacement of membranes is the main reason for the limited development. When the heat method adopts an indirect heat exchange mode, the problem of serious scaling exists, and the system cannot stably run for a long time. The coupling technology is a combination of a plurality of technologies, the process flow is long, the system is complex, and the maintenance difficulty is greatly increased. Direct contact evaporation has no partition wall for heat transfer, is not afraid of scaling, has stable process and can stably run for a long time.
The direct contact evaporation can be used for resource utilization of methane, landfill gas and the like, the required energy consumption is low, the operation cost is reduced, the equipment operation and maintenance are simple, the treatment process is simple, the flow is short, and the required cost is low.
The waste heat of the traditional direct contact evaporation process is serious, and the phenomenon that liquid drops are carried by flue gas in the evaporation process is serious, so that the contents of COD (chemical oxygen demand), ammonia nitrogen and the like in the condensate are increased.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the problem of too large energy consumption when handling high-salt organic waste water, based on the existing technology, provide a high-salt organic waste water evaporation plant. The process can fully utilize the waste heat of the high-temperature flue gas generated by the combustion chamber after passing through the high-temperature evaporation equipment, thereby reducing the energy consumption of the system and the running cost of the system.
In order to realize the technical purpose, the utility model adopts the following technical scheme:
an evaporation apparatus for high-salt organic wastewater, comprising:
a cryogenic vaporizer apparatus, comprising:
a first evaporation chamber and disposed on the first evaporation chamber:
the first feeding hole is formed in one side of the top of the first evaporation chamber;
the first liquid discharge port is positioned at the bottommost part of the first evaporation chamber;
the third feeding port is arranged at the top of the first evaporation chamber and is close to the first feeding port;
the second exhaust port is arranged on the other side of the top of the first evaporation chamber;
the bubbling chamber is arranged in the center of the first evaporation chamber, the lower end of the bubbling chamber extends into the bottom of the first evaporation chamber, and the lower part of the bubbling chamber is of a gas distribution bubbling structure;
a high temperature evaporation apparatus, comprising:
a second evaporation chamber and disposed thereon:
the second feeding hole is formed in one side of the top of the second evaporation chamber;
the second liquid outlet is positioned at the bottommost part of the second evaporation chamber;
the burner is arranged in the center of the top of the second evaporation chamber;
the combustion chamber is arranged at the bottom of the combustor and is positioned in the second evaporation chamber, and the bottom of the combustion chamber is of a gas distribution bubbling structure;
the first exhaust port is arranged on the other side of the top of the second evaporation chamber;
the fourth feeding hole is formed in the top of the second evaporation chamber and is close to the second feeding hole;
the first heat exchanger comprises a liquid inlet, a third liquid outlet, a first air inlet and a second air outlet;
a second heat exchanger comprising a second air inlet, a third air outlet, an air inlet, and an air outlet;
the first liquid discharge port on the first evaporation chamber is connected with the second feed port on the second evaporation chamber through a second circulating pump and a pipeline;
the first exhaust port on the second evaporation chamber is connected with the first air inlet on the first heat exchanger through a first separator and a pipeline;
a second exhaust port on the first heat exchanger is connected with a second air inlet on the second heat exchanger through a pipeline;
the first evaporation chamber is connected with a first heat exchanger through a first circulating pump in a pipeline manner to form a closed loop;
the second exhaust port on the first evaporation chamber is connected with a second air inlet of the second heat exchanger through a second separator pipeline;
the second liquid outlet on the second evaporation chamber is connected with the third feed inlet on the first evaporation chamber through solid-liquid separation equipment and a third circulating pump;
the first separator is connected with the upper part of the chamber wall on one side of the second evaporation chamber through a first return pipe;
the second separator is connected with the upper part of the chamber wall at one side of the first evaporation chamber through a second return pipe.
The solid-liquid separation equipment comprises first solid-liquid separation equipment, a regulating tank and second solid-liquid separation equipment which are sequentially connected in series.
And heat insulation materials are arranged outside the first evaporation chamber and the second evaporation chamber.
The high-temperature evaporation equipment and the low-temperature evaporation equipment are connected in series.
Compared with the prior art, the utility model has the advantages of it is following:
first, the utility model discloses high salt organic waste water evaporation plant, the high temperature flue gas that the combustion chamber produced gets into the knockout tower after direct contact evaporation equipment, and the knockout tower can effectively separate the liquid drop smugglied secretly in the flue gas, prevents that it from getting into the condensate, probably causes product COD, and the ammonia nitrogen value is higher. The flue gas enters a heat exchanger after passing through a separation tower, exchanges heat with high-salt organic wastewater in the low-temperature evaporation equipment, transfers heat to liquid in the low-temperature evaporation equipment, then the low-temperature flue gas after heat exchange is mixed with exhaust gas of the low-temperature evaporation equipment, and the mixed gas exchanges heat with air entering the low-temperature evaporation equipment.
And secondly, low-temperature evaporation can be used as a pretreatment part of the high-salt organic wastewater treatment system, and waste heat of high-temperature flue gas generated by the combustion chamber after passing through high-temperature evaporation equipment is fully utilized to preheat the high-salt organic wastewater and air discharged into the low-temperature evaporation equipment. The energy consumption is reduced, and the running cost of the system is reduced.
And thirdly, the direct contact evaporation and low-temperature evaporation combined operation system is characterized in that the high-temperature evaporation equipment and the low-temperature evaporation equipment are connected in series, the low-temperature evaporation equipment is positioned at the upstream section of the system, the high-salt organic wastewater is pretreated by the low-temperature evaporation equipment and then enters the high-temperature evaporation equipment for further treatment, a complex control system is not needed, the maintenance is simple, and the treatment system can stably operate for a long time.
Drawings
FIG. 1 shows a schematic diagram of the connection relationship of the high-salt organic wastewater evaporation plant of the present invention.
Description of the drawings
1, a low-temperature evaporation device, 1-1 a first feeding hole, 1-2 a first evaporation chamber, 1-3 a first liquid discharging hole, 1-4 a third feeding hole, 1-5 a second gas discharging hole and 1-6 bubbling chambers;
2 a first circulation pump for circulating the first liquid,
3 a first heat exchanger, 3-1 a liquid inlet, 3-2 a third liquid outlet, 3-3 a first air inlet and 3-4 a fourth air outlet;
4, a second circulating pump is arranged in the circulating tank,
5 high-temperature evaporation equipment, 5-1 second feeding hole, 5-2 second evaporation chamber, 5-3 second liquid discharge port, 5-4 burner, 5-5 combustion chamber and 5-6 first exhaust port;
6 a first solid-liquid separation device, 7 a regulating tank, 8 a second solid-liquid separation device, 9 a third circulating pump, 10 a first separator and 11 a first reflux pipe;
12 second heat exchanger, 12-1 second air inlet, 12-2 third air outlet, 12-3 air inlet 12-4 air outlet
13 second separator, 14 second return line.
Detailed Description
The technical solutions of the present invention will be described in detail with reference to the drawings and specific embodiments so that those skilled in the art can understand the technical solutions of the present invention more clearly.
The embodiment is as follows: reference to FIG. 1
A device for continuously treating high-salinity organic wastewater comprises a low-temperature evaporation device 1, a first circulating pump 2, a second circulating pump 4, a third circulating pump 9, a first heat exchanger 3, a second heat exchanger 12, a high-temperature evaporation device 5, a first solid-liquid separation device 6, a regulating tank 7, a second solid-liquid separation device 8, a first separator 10, a second separator 13, a first return pipe 11 and a second return pipe 14; the low-temperature evaporation equipment 1 is characterized by comprising a first feeding port 1-1, a first evaporation chamber 1-2, a first liquid discharge port 1-3, a third feeding port 1-4, a second gas discharge port 1-5 and a bubbling chamber 1-6, wherein the lower part of the bubbling chamber 1-6) is of a gas distribution bubbling structure; the high-temperature evaporation equipment is characterized by comprising a second feeding hole 5-1, a second evaporation chamber 5-2, a second liquid outlet 5-3, a combustor 5-4, a combustion chamber 5-5, a first exhaust port 5-6 and a fourth feeding hole 5-7, wherein the lower part of the combustion chamber 5-5 is of a gas distribution bubbling structure; the first heat exchanger comprises a liquid inlet 3-1, a third liquid outlet 3-2, a first air inlet 3-3 and a fourth air outlet 3-4; the second heat exchanger is characterized by comprising a second air inlet 12-1, an air outlet 12-2, an air inlet 12-3 and an air outlet 12-4.
The first liquid discharge port 1-3 is connected with a second feed port 5-1 through a second circulating pump 4 pipeline; the first exhaust port 5-6 is connected with an air inlet 3-1 of the first heat exchanger 3 through a first separator 10; a fourth exhaust port 3-4 of the first heat exchanger 5 is connected with a second inlet port 12-1 of a second heat exchanger 12 through a pipeline; the first evaporation chamber 1-2 is connected with a first heat exchanger 3 through a first circulating pump 2 in a pipeline manner to form a closed loop; the second exhaust port 1-5 is connected with a second inlet port 12-1 of a second heat exchanger 12 through a second separator 13 by a pipeline; the second liquid outlet 5-3 is connected with a third circulating pump 9 through a first solid-liquid separation device 6, an adjusting tank 7 and a second solid-liquid separation device 8, and the third feed port 1-4 is connected with the third circulating pump 9 through a pipeline.
The first separator 10 is connected with the second evaporation chamber 5-2 through a first return pipe 11 in a pipeline way, and the second separator 13 is connected with the first evaporation chamber 1-2 through a second return pipe 14 in a pipeline way.
The device of the application is adopted, and the process steps for continuously treating the high-concentration organic wastewater are as follows:
(1) Two-stage series evaporation of high-salt organic wastewater:
(1.1) the high-salt organic wastewater enters a first evaporation chamber 1-2 of the low-temperature evaporation equipment 1 from a first feeding hole 1-1; the wastewater in the first evaporation chamber 1-2 enters the first heat exchanger 3 through the liquid inlet 3-1 for preheating, is discharged from the third liquid outlet 3-2, and then returns to the first evaporation chamber 1-2 for primary evaporation after being conveyed by the first circulating pump 2;
(1.2) discharging a primary concentrated solution generated by primary evaporation from a first liquid discharge port 1-3, conveying the primary concentrated solution to a second feed port 5-1 through a second circulating pump 4, and entering a second evaporation chamber 5-2 of high-temperature evaporation equipment 5 for secondary evaporation; a secondary concentrated solution generated by secondary evaporation is discharged from a second liquid outlet 5-3 and enters a first solid-liquid separation device 6, salt mud is discharged after liquid-solid separation, and supernatant enters an adjusting tank 7 for coagulation and hardness removal; the liquid-solid mixture after the coagulation and hardness removal enters a second solid-liquid separation device 8, the salt mud is discharged after the liquid-solid separation, and the supernatant is conveyed by a third circulating pump 9 and returns to the first evaporation chamber 1-2 of the low-temperature evaporation device 2 through a third feed port 1-4 for primary evaporation.
(2) The high-temperature flue gas energy is utilized in a gradient way:
(2.1) combustible gas and combustion-supporting gas enter a combustor 5-4, are combusted in a combustion chamber 5-5, generate high-temperature flue gas, send the high-temperature flue gas into a second evaporation chamber 5-2 of high-temperature evaporation equipment 5, and carry out bubbling type direct contact heat exchange with primary concentrated solution in the second evaporation chamber 5-2, and evaporate and concentrate the primary concentrated solution; the mixed gas of the flue gas and the steam is discharged from a first exhaust port 5-6 above a second evaporation chamber 5-2, enters a first separator 10, liquid drops carried in the mixed gas are separated, the separated liquid drops are sent back to the second evaporation chamber 5-2 through a return pipe 11 for evaporation and concentration, the mixed gas enters a first heat exchanger 3 through a first gas inlet 3-3, and the wastewater in the first evaporation chamber 1-2 is preheated through primary heat exchange;
(2.2) discharging condensed water generated after primary heat exchange out of the first heat exchanger 3, discharging low-temperature mixed gas after primary heat exchange from a fourth exhaust port 3-4 of the first heat exchanger 3, entering the second heat exchanger 12 through a second air inlet 12-1 of the second heat exchanger, and preheating air through secondary heat exchange;
(2.3) discharging condensed water generated after secondary heat exchange out of the second heat exchanger 12, and discharging low-temperature mixed gas after secondary heat exchange out of the second heat exchanger 12; the preheated air in the second heat exchanger 12 enters the first evaporation chamber 1-2 of the low-temperature evaporation equipment 1, and is subjected to bubbling type direct contact heat exchange with the wastewater in the first evaporation chamber 1-2, so that the wastewater is preliminarily evaporated and concentrated; the mixed gas of air and steam is discharged from a second exhaust port 1-5 above the first evaporation chamber 1-2, enters a second separator 13, liquid drops carried in the mixed gas are separated, the separated liquid drops are sent back to the first evaporation chamber 1-2 through a second return pipe 14 for evaporation and concentration, the mixed gas enters a second heat exchanger 12, and the air is preheated through heat exchange; condensed water generated after heat exchange is discharged out of the second heat exchanger 12, and low-temperature mixed gas after heat exchange is discharged out of the second heat exchanger 12.
Starting the process and the equipment: high-salt organic wastewater is added into a second evaporation chamber 5-2 from a fourth feeding port 5-7 of a high-temperature evaporation device 5, is added into a first evaporation chamber 1-2 from a first feeding port 1-1 of a low-temperature evaporation device 1, simultaneously a combustor 5-4 starts to work, high-temperature smoke in the combustion chamber 5-5 above the second evaporation chamber 5-2 is discharged into liquid in the second evaporation chamber 5-2, then the smoke is bubbled and discharged, liquid steam is taken out and enters a first exhaust port 5-6 above the second evaporation chamber 5-2, when the system runs stably, the temperature of the discharged smoke is 70-90 ℃, a separator is arranged in an exhaust pipeline, and the smoke enters a first heat exchanger 3 after passing through a first separator 10;
when the second evaporation chamber 5-2 operates stably, namely the pressure in the evaporation chamber is stable, or the exhaust temperature is 70 to 90 ℃, starting the first circulating pump 2 to ensure that the smoke discharged by the first separator 10 exchanges heat with the high-salt organic wastewater in the first evaporation chamber 1-2, transferring the heat to the wastewater in the first evaporation chamber 1-2, when the operation is stable, namely the temperature of the wastewater in the first evaporation chamber 1-2 is 50 to 55 ℃, then discharging the low-temperature smoke subjected to heat exchange by the heat exchanger 3 from the fourth exhaust port 3-4 at the temperature of 53 to 58 ℃ to mix with the gas discharged by the first evaporation chamber 1 after passing through the second separation tower 13, the exhaust temperature of a second exhaust port 1-5 of the first evaporation chamber 1 is 47-52 ℃, the mixed gas exchanges heat with normal-temperature air entering the first evaporation chamber 1-2 through a second heat exchanger 12, the heated air enters the wastewater of the first evaporation chamber 1-2 for low-temperature evaporation, heat insulation materials are additionally arranged outside the first evaporation chamber and the second evaporation chamber to prevent heat dissipation, and the high-salt organic wastewater is preliminarily treated by the low-temperature evaporation equipment 1, discharged through a first liquid outlet 1-3 at the lower part of the low-temperature evaporation equipment 1 and further treated by a second circulating pump 4, so that the pretreated primary concentrated solution enters the high-temperature evaporation equipment 5 again.
The wastewater is treated by a high-temperature evaporation device 5 and then discharged from a second liquid outlet 5-3, enters a first solid-liquid separation device 6, is subjected to preliminary solid-liquid separation and then enters an adjusting tank 7, and is subjected to coagulation and hardness removal;
the liquid-solid mixture after the coagulation and hardness removal enters a second solid-liquid separation device 8, the salt mud is discharged after the liquid-solid separation, and the supernatant is conveyed by a third circulating pump 9 and returns to the first evaporation chamber 1-2 of the low-temperature evaporation device 2 through a third feed port 1-4 for primary evaporation.
Stable operation of the process and equipment, i.e. small temperature fluctuation or basically stable evaporation chamber pressure:
high-salt organic wastewater is added into a first evaporation chamber 1-2 from a first feeding hole 1-1 of a low-temperature evaporation device 1, the high-salt organic wastewater is primarily treated by the low-temperature evaporation device 1 and then discharged from a first liquid discharge hole 1-3 at the lower part of the low-temperature evaporation device 1, and a pretreated primary concentrated solution enters a high-temperature evaporation device 5 again for further treatment through a second circulating pump 4.
The wastewater is treated by a high-temperature evaporation device 5 and then discharged from a second liquid outlet 5-3, enters a first solid-liquid separation device 6, is subjected to preliminary solid-liquid separation and then enters an adjusting tank 7, and is subjected to coagulation and hardness removal;
and the liquid-solid mixture after the coagulation and hardness removal enters a second solid-liquid separation device 8, the salt slurry is discharged after the liquid-solid separation, and the supernatant is conveyed by a third circulating pump 9 and returns to the first evaporation chamber 1-2 of the low-temperature evaporation device 2 through a third feed port 1-4 for primary evaporation.
Claims (4)
1. A high salt organic waste water evaporation plant, characterized by comprising:
cryogenic evaporation apparatus (1), comprising:
a first evaporation chamber (1-2) and, arranged on the first evaporation chamber (1-2):
the first feeding hole (1-1) is arranged on one side of the top of the first evaporation chamber (1-2);
the first liquid discharge port (1-3) is positioned at the bottommost part of the first evaporation chamber (1-2);
the third feeding port (1-4) is arranged at the top of the first evaporation chamber (1-2) and is close to the first feeding port (1-1);
the second exhaust port (1-5) is arranged on the other side of the top of the first evaporation chamber (1-2);
the bubbling chamber (1-6) is arranged in the center of the first evaporation chamber (1-2), the lower end of the bubbling chamber extends into the bottom of the first evaporation chamber (1-2), and the lower part of the bubbling chamber (1-6) is of a gas distribution bubbling structure;
high-temperature evaporation apparatus (5) comprising:
a second evaporation chamber (5-2) and, arranged on the second evaporation chamber (5-2):
the second feeding hole (5-1) is formed in one side of the top of the second evaporation chamber (5-2);
a second liquid outlet (5-3) positioned at the bottommost part of the second evaporation chamber (5-2);
a burner (5-4) arranged at the top center of the second evaporation chamber (5-2);
the combustion chamber (5-5) is arranged at the bottom of the combustor (5-4) and is positioned in the second evaporation chamber (5-2), and the bottom of the combustion chamber (5-5) is of a gas distribution bubbling structure;
the first exhaust port (5-6) is arranged on the other side of the top of the second evaporation chamber (5-2);
a fourth feeding hole (5-7) which is arranged at the top of the second evaporation chamber (5-2) and is close to the second feeding hole (5-1);
the first heat exchanger comprises a liquid inlet (3-1), a third liquid outlet (3-2), a first air inlet (3-3) and a fourth air outlet (3-4);
a second heat exchanger including a second air inlet (12-1), a third air outlet (12-2), an air inlet (12-3), and an air outlet (12-4);
wherein, a first liquid discharge port (1-3) on the first evaporation chamber (1-2) is connected with a second feed port (5-1) on the second evaporation chamber (5-2) through a second circulating pump (4) and a pipeline;
the first exhaust port (5-6) on the second evaporation chamber (5-2) is connected with the first air inlet (3-3) on the first heat exchanger (3) through a first separator (10) and a pipeline;
a fourth exhaust port (3-4) on the first heat exchanger (3) is connected with a second air inlet (12-1) on the second heat exchanger (12) through a pipeline;
the first evaporation chamber (1-2) is connected with the first heat exchanger (3) through a first circulating pump (2) in a pipeline manner to form a closed loop;
the second exhaust port (1-5) on the first evaporation chamber (1-2) is connected with a second air inlet (12-1) of the second heat exchanger (12) through a second separator (13) by a pipeline;
the second liquid outlet (5-3) on the second evaporation chamber (5-2) is connected with the third feed inlet (1-4) on the first evaporation chamber through solid-liquid separation equipment and a third circulating pump (9);
the first separator (10) is connected with the upper part of the chamber wall at one side of the second evaporation chamber (5-2) through a first return pipe (11);
the second separator (13) is connected with the upper part of the chamber wall at one side of the first evaporation chamber (1-2) through a second return pipe (14).
2. The high-salt organic wastewater evaporation device according to claim 1, wherein the solid-liquid separation equipment comprises a first solid-liquid separation equipment, a regulating tank and a second solid-liquid separation equipment which are connected in series in sequence.
3. The high-salt organic wastewater evaporation device of claim 1, wherein the first evaporation chamber and the second evaporation chamber are externally provided with a thermal insulation material.
4. The high-salt organic wastewater evaporation plant of claim 1, wherein the high-temperature evaporation equipment is connected in series with the low-temperature evaporation equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220977427.7U CN217757159U (en) | 2022-04-26 | 2022-04-26 | High-salt organic wastewater evaporation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220977427.7U CN217757159U (en) | 2022-04-26 | 2022-04-26 | High-salt organic wastewater evaporation device |
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| Publication Number | Publication Date |
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| CN217757159U true CN217757159U (en) | 2022-11-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202220977427.7U Active CN217757159U (en) | 2022-04-26 | 2022-04-26 | High-salt organic wastewater evaporation device |
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| Country | Link |
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| CN (1) | CN217757159U (en) |
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2022
- 2022-04-26 CN CN202220977427.7U patent/CN217757159U/en active Active
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