Strong brine low-temperature evaporation system
By improving the low-temperature evaporation system for concentrated brine, the water discharged from the concentrated brine circulating pump is connected to the cooling water inlet of the second-stage separator of the ammonia evaporation tower, and the cooling water is directly or indirectly connected to the low-temperature evaporation tower, solving the problem of high energy consumption of the low-temperature evaporation system for concentrated brine in coking production, achieving significant energy saving effects.
Patent Information
- Application Number
- CN202422305843.4
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-23
- Publication Date
- 2025-07-25
- Estimated Expiration
- 2034-09-23
AI Technical Summary
The low-temperature evaporation system of concentrated brine in coking production consumes high energy, and the cooling water of the second-stage condenser of the ammonia evaporation tower consumes a lot, making it difficult for the existing technology to effectively save energy.
After changing the low-temperature evaporation system of concentrated brine to a low-temperature evaporation tower, the concentrated brine circulation pump, the primary preheater, the second-stage separator of the ammonia evaporate tower and the secondary heater, the cooling water of the second-stage separator is used to directly or indirectly connect the low-temperature evaporate tower, eliminating the cooling water of the secondary heater and the second-stage separator of the ammonia evaporate.
It significantly saves steam consumption by 2880 tons/month and coolant water consumption by 57600 tons/month, achieving significant energy-saving effects.
Smart Images
Figure CN223150325U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the wastewater treatment in coking production, in particular to a low-temperature evaporation system for concentrated brine in wastewater treatment, belonging to the technical field of wastewater treatment. Background Art
[0002] In the treatment of coking wastewater, the low-temperature evaporation system for concentrated brine is as shown in the attached... Figure 2 It is carried out by using a low-temperature evaporation tower, primary heating, and secondary heating cycle. The concentrated brine enters the low-temperature evaporation tower and is pumped into the primary preheater by a concentrated brine circulation pump to be heated to 50 to 55 degrees Celsius, and then enters the secondary heater to be heated to 70 to 80 degrees Celsius by steam and then recycled into the low-temperature evaporation tower. Taking the production scale of about 1 million tons of the applicant as an example, the steam consumption of the secondary heating in the low-temperature evaporation system is 4 tons per hour, and the monthly steam consumption is about 2,880 tons. Obviously, this requires a significant energy input. At the same time, in the ammonia distillation tower in the coking production process, cooling water needs to be introduced into the second-stage partial condenser of the ammonia distillation tower for cooling, and the cooling water consumption is about 80 tons per hour, and the monthly cooling water consumption is about 57,600 tons. Moreover, the process temperatures of the second-stage partial condenser and the concentrated brine secondary heater are similar. If the concentrated brine can be introduced into the second-stage partial condenser for heating after coming out of the primary preheater, not only can a large amount of steam be saved, but also the cooling water consumed by the second-stage partial condenser can be saved, achieving a multiplier energy-saving effect. Summary of the Invention
[0003] The utility model aims to overcome the problems of energy consumption in the low-temperature evaporation of concentrated brine and the second-stage partial condenser of the ammonia distillation tower in coking production, and provides a low-temperature evaporation system for concentrated brine.
[0004] To achieve the purpose of the utility model, the following technical solutions are adopted: A low-temperature evaporation system for concentrated brine includes a low-temperature evaporation tower. After the low-temperature evaporation tower, it is connected to the inlet of a concentrated brine circulation pump through pipelines and valves. The outlet of the concentrated brine circulation pump is connected to the inlet of a primary preheater through pipelines and valves. The outlet of the primary preheater is connected to the cooling water inlet of the second-stage partial condenser of the ammonia distillation tower through pipeline valves. The cooling water outlet of the second-stage partial condenser is directly or indirectly connected to the low-temperature evaporation tower through pipelines and valves.
[0005] Furthermore, the cooling water outlet of the second-stage partial condenser is connected to the inlet of a secondary heater, and the outlet of the secondary heater is connected to the low-temperature evaporation tower.
[0006] Furthermore, a connection is made between the outlet of the primary preheater and the inlet of the secondary heater through pipelines and valves.
[0007] This system has a significant energy-saving effect, basically eliminating all the steam used in the existing secondary heater, and completely eliminating the cooling water used in the second-stage partial condenser of the ammonia distillation tower, which will be specifically described in detail in combination with the specific embodiments. Brief Description of the Drawings
[0008] Figure 1 is a schematic diagram of the present utility model.
[0009] Figure 2 is a schematic diagram of the original low-temperature evaporation system. Detailed Description of the Preferred Embodiment
[0010] To more fully explain the implementation of the present utility model, implementation examples of the present utility model are provided. These implementation examples are merely illustrative of the present utility model and do not limit the scope of the present utility model.
[0011] The present utility model will be further explained in detail with reference to the accompanying drawings. The reference numerals in the drawings are as follows: 1: low-temperature evaporation tower; 2: concentrated brine circulation pump; 3: primary preheater; 4: secondary heater; 5: second-stage fractionator; 6: pipeline A; 7: pipeline B; 8: pipeline C; 9: pipeline D; 10: pipeline E; 11: pipeline F.
[0012] As shown in the Figure 1 drawings, a low-temperature evaporation system for concentrated brine includes a low-temperature evaporation tower 1. After the low-temperature evaporation tower, it is connected to the inlet of the concentrated brine circulation pump 2 through pipelines and valves. In the figure, pipeline A6 is the connecting pipeline between the low-temperature evaporation tower and the concentrated brine circulation pump. The outlet of the concentrated brine circulation pump is connected to the inlet of the primary preheater 3 through pipelines and valves. In the figure, pipeline B7 is the connecting pipeline between the concentrated brine circulation pump and the primary preheater. The outlet of the primary preheater is connected to the cooling water inlet of the second-stage fractionator of the ammonia stripping tower through pipeline valves. In the figure, pipeline C8 is the connecting pipeline between the primary preheater and the second-stage fractionator. The cooling water outlet of the second-stage fractionator 5 is directly or indirectly connected to the low-temperature evaporation tower through pipelines and valves. In this embodiment, the cooling water outlet of the second-stage fractionator 5 is connected to the inlet of the secondary heater 4. In the figure, pipeline D9 is the connecting pipeline between the second-stage fractionator and the secondary heater. The outlet of the secondary heater 4 is connected to the low-temperature evaporation tower 1. In the figure, pipeline E10 is the connecting pipeline between the secondary heater and the low-temperature cooling tower. There is a connection between the outlet of the primary preheater and the inlet of the secondary heater through pipelines and valves. In the figure, pipeline F11 is the connecting pipeline between the primary preheater and the secondary heater.
[0013] Figure 1Based on the existing system, the water outlet of the primary preheater in the shown system is connected to the water inlet of the secondary fractionator, and the water outlet of the secondary fractionator is then connected to the secondary heater. When the ammonia distillation tower is operating normally, the valve on the pipeline between the primary preheater and the secondary heater is closed. The water outlet after passing through the primary preheater enters the secondary fractionator for cooling. While being cooled, the concentrated brine itself heats up to about 80 degrees Celsius and then enters the secondary heater. When the ammonia distillation tower is operating normally, the heating steam of the secondary heater is closed, and the concentrated brine enters the low-temperature evaporation tower after passing through the secondary heater. There are two functions retained for the secondary heater in this system. One is that when the ammonia distillation tower is under maintenance, steam can be introduced into the secondary heater for heating (i.e., the existing operation process). The other is to prevent the situation where the concentrated brine cannot be heated to the set temperature through the secondary fractionator in case of too low temperature in winter. In this case, a small amount of steam can be introduced into the secondary heater to heat it to the set temperature.
[0014] By adopting this system, the monthly steam saving is about 2,880 tons, and the monthly cooling water consumption saving is 57,600 tons, showing remarkable energy-saving effects.
[0015] After elaborating on the implementation mode of the present utility model in detail, those familiar with the technology can clearly understand that various changes and modifications can be made without departing from the above-mentioned scope and spirit of the patent application. Any simple modification, equivalent change, and modification made to the above embodiments based on the technical essence of the present utility model all belong to the scope of the technical solution of the present utility model, and the present utility model is not limited to the implementation modes of the examples given in the specification either.
Claims
1. A low-temperature evaporation system for concentrated brine, comprising a low-temperature evaporation tower. After the low-temperature evaporation tower, the inlet water of a concentrated brine circulation pump is connected through pipelines and valves. The outlet water of the concentrated brine circulation pump is connected to the inlet water of a primary preheater through pipelines and valves. It is characterized in that: The water outlet of the primary preheater is connected to the cooling water inlet of the second-stage fractionator of the ammonia distillation column through pipeline valves, and the cooling water outlet of the second-stage fractionator is directly or indirectly connected to the low-temperature evaporation tower through pipelines and valves.
2. The low-temperature evaporation system for concentrated brine according to claim 1, wherein: The cooling water outlet of the second-stage fractionator is connected to the water inlet of the secondary heater, and the water outlet of the secondary heater is connected to the low-temperature evaporation tower.
3. The low-temperature evaporation system for concentrated brine according to claim 1, wherein: The water outlet of the primary preheater and the water inlet of the secondary heater are connected through pipelines and valves.