Water-vapor separation device for sodium carbonate production
By combining multi-stage heat exchangers and gas-liquid separation equipment, the problem of increased mother liquor volume caused by ammonia absorbing moisture in soda ash production was solved, achieving efficient cooling and energy reuse, and improving production efficiency and product quality.
Patent Information
- Application Number
- CN202520272603.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-02-20
- Publication Date
- 2026-01-30
- Estimated Expiration
- 2035-02-20
AI Technical Summary
In the existing soda ash production process, the temperature of the gas in the lower stage is high after it passes through the compressor and needs to be cooled down. However, the direct seawater spraying process causes ammonia to absorb moisture, increasing the amount of mother liquor and increasing steam consumption.
The system employs multi-stage heat exchangers and gas-liquid separation equipment. The lower-stage gas is cooled sequentially through the first, second, and third heat exchangers, while the gas-liquid separation equipment separates the moisture, preventing ammonia from absorbing moisture. The recovery equipment also recovers heat.
It effectively reduces the temperature of the lower air section, avoids water absorption during the cooling process, improves the cooling effect, reduces energy waste, improves energy utilization, reduces production costs, and enhances product quality and output.
Smart Images
Figure CN223846614U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to a chemical industry field especially relates to a soda production water vapor separation device. BACKGROUND
[0002] Soda is an important basic chemical product, is widely used in glass, chemical industry, enamel, papermaking, printing and dyeing etc. field, holds an important position in national economy, with the steady growth of economy and the development of domestic and international market, the demand of soda product is rising constantly, the industry prospect is broad.
[0003] The soda production water vapor separation device still has the following defects when in use: the existing soda production lower section gas is compressed by the compressor and has high temperature, needs to be cooled before entering the carbonization tower, the current adopted process is sea water direct spraying process, although simple easy operation, cooling effect is good, but because lower section gas contains a certain amount of ammonia gas, can lead to ammonia gas absorbs moisture, and then brings into the carbonization tower, increases the mother liquor amount, and then increases the steam consumption of subsequent mother liquor ammonia absorption link. UTILITY MODEL CONTENT
[0004] The utility model aims at solving the shortcomings in the prior art and provides a soda production water vapor separation device.
[0005] In order to realize the above-mentioned purpose, the utility model adopts the following technical scheme: a soda production water vapor separation device, including the compressor, be equipped with the first heat exchanger on the compressor, the first heat exchanger below is equipped with the second heat exchanger, the second heat exchanger below is equipped with the third heat exchanger, the second heat exchanger one side is equipped with the gas water separation equipment, the gas water separation equipment below is equipped with the recovery equipment, the gas water separation equipment is fixedly connected with the conveying pipe.
[0006] Further description of the above technical scheme: the outlet of the compressor is connected with the inlet of the first heat exchanger through a pipeline, and the outlet of the first heat exchanger is connected with the third heat exchanger through a pipeline.
[0007] Further description of the above technical scheme: the outlet of the compressor is connected with the inlet of the second heat exchanger through a pipeline, and the outlet of the second heat exchanger is connected with the inlet of the gas water separation equipment through a pipeline.
[0008] Further description of the above technical scheme: the outlet of the compressor is connected with the inlet of the third heat exchanger through a pipeline.
[0009] Further description of the above technical scheme: one end of the conveying pipe is connected to the inlet of the carbonization tower.
[0010] As a further description of the above technical solution: the inlet of the compressor is connected with the light ash furnace gas outlet of the calcination workshop through a pipeline.
[0011] As a further description of the above technical solution: the light ash furnace gas is compressed to 0.32-0.38 MPa in the compressor.
[0012] The utility model has the advantages of the following beneficial effects:
[0013] 1. In the utility model, the temperature of the lower section gas is effectively reduced through the sequential cooling of the first heat exchanger, the second heat exchanger and the third heat exchanger, and the problem of water absorption in the cooling process caused by ammonia is avoided, thereby ensuring the maximization of the cooling effect, the recovery equipment can recover the heat in the separated moisture, and the heat can be reused in other production links, thereby reducing the waste of energy and improving the overall energy utilization rate, which not only helps to reduce the production cost, but also promotes sustainable development.
[0014] 2. In the utility model, the moisture in the lower section gas is effectively separated by the gas-water separation equipment, the water content in the lower section gas is reduced, and the liquid equivalent in the carbonization tower is directly reduced, so that the treatment process of the carbonization tower is more efficient, the lower section gas with reduced water content can participate in the chemical reaction more fully after entering the carbonization tower, and the quality and yield of the product are improved, and meanwhile, the problems of increased equipment load and rising energy consumption caused by excessive moisture are reduced. BRIEF DESCRIPTION OF DRAWINGS
[0015] Figure 1 A structure diagram of a soda production water vapor separation device is provided for the utility model.
[0016] LEGEND:
[0017] 1. Compressor; 2. First heat exchanger; 3. Second heat exchanger; 4. Third heat exchanger; 5. Gas-water separation equipment; 6. Recovery equipment; 7. Delivery pipe. DETAILED DESCRIPTION
[0018] The technical solutions in the embodiments of the utility model will be described clearly and completely below with reference to the drawings in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, rather than all the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by those skilled in the art without creative labor fall within the scope of protection of the utility model.
[0019] REFERENCE Figure 1The utility model provides a kind of embodiment: a soda production water vapor separation device, including compressor 1, compressor 1 is equipped with first heat exchanger 2, the below of first heat exchanger 2 is equipped with second heat exchanger 3, the below of second heat exchanger 3 is equipped with third heat exchanger 4, one side of second heat exchanger 3 is equipped with gas-water separation equipment 5, the below of gas-water separation equipment 5 is equipped with recovery equipment 6, gas-water separation equipment 5 is fixedly connected with conveying pipe 7, by the cooling of first heat exchanger 2, second heat exchanger 3 and third heat exchanger 4 in turn, the temperature of lower section gas has been effectively reduced, and this process avoids the problem of water absorption in cooling process due to ammonia content, to ensure the maximization of cooling effect, recovery equipment 6 can recover the heat in separated moisture, this part of heat can be reused in other production links, to reduce the waste of energy, improve overall energy utilization, not only help to reduce production cost, but also sustainable development.
[0020] The outlet of compressor 1 is connected with the inlet of first heat exchanger 2 through pipeline, the outlet of first heat exchanger 2 is connected with third heat exchanger 4 through pipeline, the outlet of compressor 1 is connected with the inlet of second heat exchanger 3 through pipeline, the outlet of second heat exchanger 3 is connected with the inlet of gas-water separation equipment 5 through pipeline, the outlet of compressor 1 is connected with the inlet of third heat exchanger 4 through pipeline, one end of conveying pipe 7 is connected with the inlet of carbonization tower, the inlet of compressor 1 is connected with the light ash furnace gas outlet of calcination workshop through pipeline, the light ash furnace gas is compressed to 0.32-0.38MPa in compressor 1, gas-water separation equipment 5 effectively separates moisture in lower section gas, reduces the moisture content in lower section gas, directly reduces the liquid equivalent in carbonization tower, so that the processing process of carbonization tower is more efficient, the lower section gas with reduced moisture content can more fully participate in chemical reaction after entering carbonization tower, improves the quality and yield of product, at the same time, reduces the problems of equipment load increase and energy consumption rise caused by excessive moisture.
[0021] Working principle: in use, the outlet of the compressor 1 is connected with the inlet of the first heat exchanger 2 through a pipeline, the lower section gas is compressed by the compressor and then enters the first heat exchanger for preliminary cooling, the preliminarily cooled lower section gas enters the third heat exchanger 4 for further cooling through the outlet of the first heat exchanger 2 and the pipeline, at the same time, the outlet of the compressor 1 can also be directly connected with the inlet of the second heat exchanger 3 through a pipeline, and the lower section gas is cooled through the first heat exchanger 2 and the second heat exchanger 3, the lower section gas cooled from the second heat exchanger 3 enters the gas-water separation device 5 for gas-water separation, in the process, the water in the lower section gas is separated out and recycled through the recycling device 6, the separated lower section gas is transported to the carbonization tower through the conveying pipe 7 for further treatment, and one end of the conveying pipe 7 is connected to the inlet of the carbonization tower, so as to ensure that the lower section gas can smoothly enter the carbonization tower, the sequential cooling through the first heat exchanger 2, the second heat exchanger 3 and the third heat exchanger 4 can more effectively reduce the temperature of the lower section gas, and at the same time, the problem that the lower section gas absorbs water in the cooling process due to containing ammonia is avoided, the water in the lower section gas is separated by the gas-water separation device 5, the water content in the lower section gas is reduced, and thus the liquid equivalent in the carbonization tower is reduced, which is helpful for reducing the steam consumption in the mother liquor ammonia evaporation process, the heat in the separated water is recycled through the recycling device 6, so that the energy can be recycled, and the overall energy utilization rate is improved.
[0022] Finally, it should be pointed out that: the above only preferred embodiments of the present application, and not for limiting the present application, although the foregoing detailed description of the present application, for the person skilled in the art, it still can be modified, or part of the technical features of the equivalent replacement, within the spirit and principles of the present application, any modification, equivalent replacement, improvement, etc., should be included in the scope of protection of the present application.
Claims
1. A soda production water vapor separation device comprising a compressor (1), characterized in that: The compressor (1) is provided with a first heat exchanger (2), the lower side of the first heat exchanger (2) is provided with a second heat exchanger (3), the lower side of the second heat exchanger (3) is provided with a third heat exchanger (4), one side of the second heat exchanger (3) is provided with a gas-water separation device (5), the lower side of the gas-water separation device (5) is provided with a recovery device (6), and the gas-water separation device (5) is fixedly connected with a conveying pipe (7).
2. The water vapor separation device for soda production according to claim 1, characterized in that: The outlet of the compressor (1) is connected with the inlet of the first heat exchanger (2) through a pipeline, and the outlet of the first heat exchanger (2) is connected with the third heat exchanger (4) through a pipeline.
3. The water vapor separation device for soda production according to claim 2, characterized in that: The outlet of the compressor (1) is connected with the inlet of the second heat exchanger (3) through a pipeline, and the outlet of the second heat exchanger (3) is connected with the inlet of the gas-water separation device (5) through a pipeline.
4. The soda production water vapor separation device according to claim 3, characterized in that: The outlet of the compressor (1) is connected with the inlet of the third heat exchanger (4) through a pipeline.
5. The water-steam separation device for soda production according to claim 4, characterized in that: One end of the conveying pipe (7) is connected with the inlet of the carbonization tower.
6. The soda production water vapor separation device according to claim 5, characterized in that: The inlet of the compressor (1) is connected with the light ash furnace gas outlet of the calcination workshop through a pipeline.
7. The soda production water vapor separation device according to claim 6, characterized in that: The light ash furnace gas is compressed to 0.32-0.38 MPa in the compressor (1).