Treatment system and method for discharging alkali liquor from sodium carbonate

Abstract

The invention discloses a processing system and method for discharging alkali liquor from sodium carbonate, and belongs to the technical field of chemical engineering, the processing system for discharging alkali liquor from sodium carbonate comprises a distributing device and a conveying mechanism which are sequentially connected, and a washing water circulating system, a belt filter and a medium wave infrared device are sequentially arranged in the direction of conveying alkali liquor from sodium carbonate by the conveying mechanism; the washing water circulation system comprises a first-section washing water mechanism, a second-section washing water mechanism and a third-section washing water mechanism which are sequentially arranged, then third-section washing water treatment, belt filter treatment and medium-wave infrared treatment are sequentially carried out on the soda outlet liquor, the third-section washing water is additionally arranged through gradient heat exchange utilization of desalted water, and a third-section washing water circulation system is constructed. According to the present invention, with the combination of the filter aid compounding and the medium-wave infrared radiation reinforced dehydration, the filtration condition is optimized from the source, such that the purposes of filter cake moisture reducing, filtration pressure difference reducing, equipment scaling relieving and washing efficiency improving are achieved so as to reduce the calcination energy consumption, improve the product purity, prolong the equipment operation period and reduce the maintenance cost;

Description

Technical Field

[0001] This application relates to the field of chemical technology, specifically to a system and method for treating soda ash efflorescence. Background Technology

[0002] In the ammonia-soda process for soda ash production, heavy alkali filtration is a crucial step, and the moisture content of the filter cake directly impacts the medium-pressure steam consumption and production capacity of the calcining furnace. The medium-pressure steam equivalent in the calcining furnace is approximately 1.35 t / t of alkali, accounting for about 18% of the total energy consumption of soda ash production—a significant proportion. Currently, the soda ash industry is highly competitive; therefore, efforts should be made to reduce the moisture content of the heavy alkali filter cake. This not only saves on the medium-pressure steam cost in the calcining furnace but also greatly benefits the improvement of the furnace's production capacity.

[0003] The separation of heavy alkali is the core link in the production of soda ash (sodium carbonate). Its goal is to efficiently separate sodium bicarbonate (heavy alkali) crystals and mother liquor from the carbonated alkali solution, which directly affects product quality, energy consumption and production cost. The current process flow of the traditional mechanical separation system is as follows: the crystal slurry flowing out from the bottom of the carbonation tower enters the alkali solution tank, and is separated into solid and liquid by a vacuum filter. The filter cake is washed, dehydrated and sent to the calcination process to produce soda ash. The process equipment includes an alkali solution tank, a rotary drum filter, a high-level washing water tank, a belt conveyor and a vacuum pump system. Its core principle relies on the vacuum negative pressure to drive the formation of a pressure difference on both sides of the filter cloth. The mother liquor is drawn away while the heavy alkali is retained on the filter screen. The typical rotary drum filter working cycle covers seven steps: suction-drying-washing-squeezing-secondary suction-scraping-air cleaning. It has the following disadvantages: (1) The filter cake has a high moisture content: about 18-19%, which leads to a large consumption of downstream calcination steam. (2) Energy consumption and washing water consumption: The vacuum pump has high power (e.g., 7.5kW level), and the washing water equivalent is >600 kg / t alkali. (3) Production capacity limitation: The processing capacity is low, and it depends on manual operation to adjust parameters.

[0004] Traditional vacuum drum filtration technology has low production capacity, large wash water equivalent, and high moisture content in the heavy alkali filter cake, resulting in high steam consumption in the downstream calcination process, reaching 1.45 tons of steam per ton of alkali. A 300,000-ton soda ash plant consumes over 40,000 tons of steam energy under medium pressure. Applying advanced heavy alkali filtration technology will help promote energy conservation and emission reduction in the soda ash industry.

[0005] Therefore, this application is submitted. Summary of the Invention

[0006] The purpose of this invention is to overcome the shortcomings of the existing technology and provide a soda ash efflorescence treatment system and method.

[0007] To achieve the above objectives, the technical solution adopted by the present invention is as follows: A soda ash efflux treatment system includes a distributor and a conveying mechanism connected in sequence. A washing water circulation system, a belt filter and a medium-wave infrared device are arranged in sequence along the direction of conveying soda ash efflux from the conveying mechanism. The washing water circulation system includes a first-stage washing mechanism, a second-stage washing mechanism, and a third-stage washing mechanism arranged sequentially. The first-stage washing mechanism includes a first-stage washing water pipe, a mother liquor separator, and a mother liquor tank connected in sequence. The second-stage washing water pipe includes a second-stage washing water pipe, a washing water separator, a first-stage washing water tank, and a first-stage washing water pump connected in sequence. The first-stage washing water pump is used to connect the first-stage washing water tank and the first-stage washing water pipe. The third-stage washing mechanism includes a vacuum machine, a multi-purpose tank, a demineralized water circulation pump, a filtered tail gas ammonia purification tower, a calcined tail gas ammonia purification tower, a high-level tank, a third-stage washing water pipe, a second-stage washing water tank, and a second-stage washing water pump connected in sequence. The second-stage washing water pump is used to connect the second-stage washing water tank and the second-stage washing water pipe.

[0008] Preferably, it also includes a filter aid tank and a filter aid pump connected in sequence, wherein the filter aid pump is connected to the three sections of washing water pipes.

[0009] Preferably, the outlet of the mother liquor separator is connected to the ammonia purification tower for filtered tail gas.

[0010] Preferably, the washing water separator and the gas outlet are connected to the filtered tail gas ammonia purification tower.

[0011] Preferably, the high-level slot is also connected to the multi-purpose slot.

[0012] Preferably, a buffer tank is provided between the filtered tail gas ammonia purification tower and the calcined tail gas ammonia purification tower; A wash water booster pump is also provided between the two-stage wash water pump and the two-stage water supply pipeline.

[0013] The present invention also provides a method for treating soda ash efflorescence, based on the above-described soda ash efflorescence treatment system, comprising the following steps: S1: After the demineralized water undergoes the first heat exchange in the vacuum machine, it is sent to the multi-purpose tank. Then, it is sent to the ammonia purification tower of the filtered tail gas and the ammonia purification tower of the calcined tail gas in sequence by the demineralized water circulation pump for the second and third heat exchanges. The demineralized water after heat exchange is sent to the high-level tank. S2: The soda ash effluent is evenly distributed on the conveying structure by the distributor. It passes through a first-stage washing, a second-stage washing, and a third-stage washing in sequence along the direction of movement of the conveying mechanism. The third-stage washing water is mixed with the filter aid in a certain proportion and then used to wash the heavy soda ash filter cake. After that, it is processed by a belt filter and finally calcined by penetrating radiation heating through a medium-wave infrared device.

[0014] Preferably, the dosage of the filter aid is 0.02~0.04 kg / m³. 3 The filter aid is a sulfonate copolymer.

[0015] Preferably, the temperature of the penetrating radiation heating is 85~90℃; The temperature of the washing water in this section is 30~35℃, and the dosage is 20~25m³. 3 / h; The temperature of the second-stage washing water is 40~45℃, and the dosage is 18~20m³. 3 / h; The temperature of the three-stage washing water is 40~45℃, and the dosage is 15~20m³. 3 / h.

[0016] Preferably, the washing liquid from the three-stage washing process passes sequentially through the second-stage washing tank and the second-stage washing pump into the second-stage washing pipeline for secondary washing. The washing liquid after the secondary washing passes sequentially through a washing water separator, a washing water tank, and a washing water pump before entering a washing water pipeline for primary washing. The washing liquid after the first water wash passes through a section of washing water pipe and a mother liquor separator before entering the mother liquor tank. The secondary wash water and its gas phase enter the filtration tail gas ammonia purification tower for treatment, and then are vented by a vacuum pump.

[0017] The beneficial effects of this invention are as follows: The soda ash efflux treatment system described in this application includes a distributor and a conveying mechanism connected in sequence. A washing water circulation system, a filter press, and a mid-wave infrared device are sequentially arranged along the direction in which the soda ash efflux is conveyed by the conveying mechanism. The washing water circulation system includes a first-stage washing mechanism, a second-stage washing mechanism, and a third-stage washing mechanism arranged in sequence, thereby sequentially treating the soda ash efflux with three-stage washing water treatment, filter press treatment, and mid-wave infrared treatment. By utilizing the stepped heat exchange of demineralized water, adding three-stage washing water, and constructing a three-stage washing water circulation system, combined with the compounding of filter aids and mid-wave infrared radiation to enhance dehydration, the filtration conditions are optimized from the source, achieving the goals of reducing filter cake moisture, reducing filtration pressure difference, alleviating equipment scaling, and improving washing efficiency. This reduces calcination energy consumption, improves product purity, extends equipment operating cycle, and reduces maintenance costs. Attached Figure Description

[0018] Figure 1 This is a schematic diagram of the soda ash alkali treatment system described in this invention.

[0019] The diagram shows the following components: 1. Fabric distributor; 2. Conveying structure; 3. First-stage washing mechanism; 31. First-stage washing pipeline; 32. Mother liquor separator; 33. Mother liquor tank; 4. Second-stage washing mechanism; 41. Second-stage washing pipeline; 42. Washing separator; 43. First-stage washing tank; 44. First-stage washing pump; 5. Third-stage washing mechanism; 51. Vacuum machine; 52. Multi-purpose tank; 53. Demineralized water circulation pump; 54. Ammonia purification tower for filtered tail gas; 55. Ammonia purification tower for calcined tail gas; 56. High-level tank; 57. Third-stage washing pipeline; 58. Second-stage washing tank; 59. Second-stage washing pump; 6. Filter press; 7. Mid-wave infrared device; 8. Filter aid tank; 9. Filter aid pump; 10. Buffer tank; 11. Washing water pressurization pump. Detailed Implementation

[0020] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions in the embodiments of this application will be clearly and completely described below. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. Based on the embodiments in this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0021] In this application, the technical features described in an open-ended manner include both closed technical solutions consisting of the listed features and open technical solutions that include the listed features.

[0022] In this application, numerical ranges are referred to as continuous unless otherwise specified, and include the minimum and maximum values ​​of the range, as well as every value between the minimum and maximum values. Furthermore, when the range refers to integers, it includes every integer between the minimum and maximum values ​​of the range. Additionally, when multiple ranges are provided to describe a feature or characteristic, the ranges may be merged. In other words, unless otherwise specified, all ranges disclosed herein should be understood to include any and all subranges to which they are incorporated.

[0023] In this application, there are no particular restrictions on the specific dispersion and mixing methods.

[0024] Unless otherwise specified, all components, raw materials, or instruments used in the embodiments and comparative examples of this invention are commercially available, and the components and raw materials used in each parallel experiment are the same.

[0025] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0026] like Figure 1 As shown in the figure, this application provides a soda ash alkali treatment system, including a feeder 1 and a conveying mechanism connected in sequence. A washing water circulation system, a filter 6 and a mid-wave infrared device 7 are arranged in sequence along the direction of conveying soda ash alkali from the conveying mechanism.

[0027] Furthermore, the washing water circulation system includes a first-stage washing mechanism 3, a second-stage washing mechanism 4, and a third-stage washing mechanism 5 arranged sequentially. The first-stage washing mechanism 3 includes a first-stage washing water pipe 31, a mother liquor separator 32, and a mother liquor tank 33 connected sequentially. The second-stage washing water pipe includes a second-stage washing water pipe 41, a washing water separator 42, a first-stage washing water tank 43, and a first-stage washing water pump 44 connected sequentially. The first-stage washing water pump 44 is used to connect the first-stage washing water tank 43 and the first-stage washing water pipe 31. The third-stage washing mechanism 5 includes a vacuum machine 51, a multi-purpose tank 52, a demineralized water circulation pump 53, a filtered tail gas ammonia purification tower 54, a calcined tail gas ammonia purification tower 55, a high-level tank 56, a third-stage washing water pipe 57, a second-stage washing water tank 58, and a second-stage washing water pump 59 connected sequentially. The second-stage washing water pump 59 is used to connect the second-stage washing water tank 58 and the second-stage washing water pipe 41.

[0028] The soda ash efflux treatment system described in this application includes a distributor 1 and a conveying mechanism connected in sequence. Along the direction of conveying the soda ash efflux from the conveying mechanism, a washing water circulation system, a filter press 6, and a mid-wave infrared device 7 are arranged in sequence. The washing water circulation system includes a first-stage washing mechanism 3, a second-stage washing mechanism 4, and a third-stage washing mechanism 5 arranged in sequence. This allows the soda ash efflux to undergo three-stage washing water treatment, filter press 6 treatment, and mid-wave infrared treatment in sequence. By utilizing the cascade heat exchange of demineralized water, adding a third-stage washing water system, and constructing a three-stage washing water circulation system, combined with filter aid compounding and mid-wave infrared radiation-enhanced dehydration, the filtration conditions are optimized from the source. This achieves the goals of reducing filter cake moisture, decreasing filtration pressure difference, alleviating equipment scaling, and improving washing efficiency, thereby reducing calcination energy consumption, increasing product purity, extending equipment operating cycles, and reducing maintenance costs.

[0029] The washing water circulation system of this application includes a first-stage washing mechanism 3, a second-stage washing mechanism 4, and a third-stage washing mechanism 5 arranged sequentially. The system is scientifically and rationally designed, with the return liquid from the third-stage washing water replenishing the second-stage washing water, and vice versa. Filter cloth cleaning wastewater also replenishes the second-stage washing water. Combined with a demineralized water cascade heat exchange utilization scheme, this achieves multi-stage water resource circulation, controlling the washing water equivalent to ≤600 kg / t alkali, further reducing washing water consumption compared to existing technologies. Simultaneously, the outlets of the mother liquor separator 32 and the ammonia purification tower 54 are connected to the ammonia purification tower 54. During the heat exchange process, the ammonia in the exhaust gas from the mother liquor separator 32 and the ammonia purification tower 54 reduces the pollutant content in the waste gas, resulting in significant environmental benefits. This advantage is achieved through a three-stage countercurrent washing and washing water circulation and recovery technology design, distinguishing it from the problems of low washing water utilization efficiency and serious waste in existing technologies.

[0030] This invention achieves a progressive purification effect through the combined treatment of three-stage washing water and filter aid. The first-stage washing water removes a large amount of mother liquor, the second-stage washing water further reduces salt content, and the third-stage washing water deeply removes impurities under the action of filter aid, ensuring that the salt content of soda ash is controlled below 0.20%. At the same time, it reduces the phenomenon of soda ash agglomeration and scaling, improves material flowability, increases the calcination rate of subsequent calcination processes, and ensures the stability of soda ash product purity.

[0031] The processing system described in this application has a single-unit production capacity of 75 t / h; the moisture content of the heavy alkali is ≤14.5%; the salinity of the heavy alkali is ≤0.5%; the wash water equivalent is ≤600 kg / t alkali; the solid recovery rate is ≥98%; and the calcination rate of the heavy alkali is ≥53%. The amount of soft water required for washing is reduced by 0.6 m³ / ton of alkali. 3 The calcination rate of heavy alkali is increased by 1%, the average moisture content decreases by 1.5%, and 60 kg of medium-pressure steam is saved per ton of alkali, showing broad application prospects.

[0032] Preferably, it also includes a filter aid tank 8 and a filter aid pump 9 connected in sequence, wherein the filter aid pump 9 is connected to the three-section washing water pipe 57.

[0033] This application incorporates a mid-wave infrared device 7 during the filtration process. By utilizing demineralized water in stages and adding filter aids, the moisture content of the filter cake is reduced, minimizing the scaling and caking of the heavy alkali, thus lowering the filtration pressure differential. By reducing filter cake moisture and improving material flowability, energy consumption during calcination is significantly reduced, and product purity is increased. Simultaneously, the staged utilization of demineralized water effectively alleviates equipment scaling and clogging problems, extends equipment operating cycles, and reduces maintenance costs.

[0034] In some embodiments, the outlet of the mother liquor separator 32 is connected to the ammonia purification tower 54 for filtered tail gas, and the outlet of the washing water separator 42 is connected to the ammonia purification tower 54 for filtered tail gas.

[0035] In some embodiments, the high-level slot 56 is also connected to the multi-purpose slot 52.

[0036] In some embodiments, a buffer tank 10 is also provided between the filtered tail gas ammonia purification tower 54 and the calcined tail gas ammonia purification tower 55.

[0037] In some embodiments, a wash water booster pump 11 is also provided between the two-stage wash water pump 59 and the two-stage water supply pipeline.

[0038] The washing water pressurization pump 11 is configured so that the water output can be used to supply the second stage of washing water, clean the filter belt and filter cloth of the conveying mechanism, and also be used as lubricating water for the wear-resistant belt and vacuum box, effectively improving the utilization rate.

[0039] The conveying mechanism is a belt conveyor.

[0040] The belt conveyor is a vacuum horizontal belt filter, product model VBF / 108B40, full name VACOOMBELT FILTER 108B40, specifications: 32930×5600×2710, vacuum coverage area: 27000×4000, filtration area: 108m². 2 Width: 4M, Vacuum degree: -0.046~-0.060MPa, Operating temperature: 32℃.

[0041] The mid-wave infrared device 7 converts electrical energy into mid-wave infrared radiation that can be directionally conducted through the air. Compared to steam used for calcination, which only directly heats the surface of the filter cake, mid-wave infrared radiation penetrates into the interior of the filter cake, is absorbed by the internal molecules, and is converted into molecular thermal motion. This molecular thermal motion generates heat, which, through heat transfer, causes the overall temperature of the filter cake to rise, increasing the rate of moisture diffusion and evaporation. Furthermore, under the synergistic effect of the vacuum suction of the filter press 6, moisture is more easily separated from the heavy alkali filter cake, thereby effectively reducing the moisture content of the heavy alkali. Using the mid-wave infrared device 7 significantly improves work efficiency, shortens the heating cycle, saves energy consumption, reduces production costs, and causes no pollution to the heated object or the environment. Compared to medium-pressure steam heating, the cost of using mid-wave infrared radiation is significantly reduced; compared to traditional quartz infrared heating technology, its installed power is lower, only about one-third of the original. This equipment truly achieves the goals of being dust-free, energy-saving, highly efficient, safe, and durable.

[0042] The mid-wave infrared device 7 (heating source SN11, 1.8KW) consists of 90 mid-wave infrared radiant heating plates, each measuring 410×300×20mm, arranged longitudinally to form a radiant heating area of ​​3400×5500mm. Each heating plate has a power of 1.8kW, with a total installed power of 162kW, enabling real-time radiant heating of the filter cake in the filter press 6.

[0043] The belt filter 6 described herein is the belt filter 6 disclosed in CN 214680451 U.

[0044] The present invention also provides a method for treating soda ash efflorescence, based on the above-described soda ash efflorescence treatment system, comprising the following steps: S1: After the first heat exchange by the vacuum machine 51, the demineralized water is sent to the multi-purpose tank 52, and then sent to the filter tail gas ammonia purification tower 54 and the calcination tail gas ammonia purification tower 55 in sequence by the demineralized water circulation pump 53 for the second and third heat exchange. The demineralized water after heat exchange is sent to the high-level tank 56. S2: The soda ash effluent is evenly distributed on the conveying structure 2 by the distributor 1. It passes through the first washing stage, the second washing stage, and the third washing stage in sequence along the direction of movement of the conveying mechanism. The third washing water is mixed with the filter aid in a certain proportion and then used to wash the heavy soda ash filter cake. Then it is processed by the belt filter 6 and finally calcined by the penetrating radiation heating of the medium-wave infrared device 7.

[0045] The processing method described in this application is based on the above-mentioned processing system, which sequentially performs three-stage washing water treatment, filter treatment, and mid-wave infrared treatment on the soda ash effluent. By utilizing the cascade heat exchange of demineralized water, adding three-stage washing water, and constructing a three-stage washing water circulation system, combined with the compounding of filter aids and mid-wave infrared radiation to enhance dehydration, the filtration conditions are optimized from the source. This achieves the goals of reducing filter cake moisture, reducing filtration pressure difference, alleviating equipment scaling, and improving washing efficiency, thereby reducing calcination energy consumption, improving product purity, extending equipment operating cycle, and reducing maintenance costs.

[0046] The cooling water for vacuum machine 51 uses demineralized water (free of calcium and magnesium ions) that has undergone staged heat exchange, replacing the easily scale-forming process water in existing technologies. This fundamentally avoids bearing scaling and equipment wear caused by calcium and magnesium ion deposition, extending the operating cycle of vacuum machine 51 and reducing downtime for maintenance and spare parts replacement costs (existing vacuum machines 51 require frequent cleaning due to scaling, resulting in higher maintenance costs). The washing water circulation system reduces salt residue on the filter cloth surface. Combined with the circulating replenishment of filter cloth cleaning wastewater, it prevents the filter cloth from being clogged by salt crystals or corroded. At the same time, the filter aid reduces the adhesion between the filter cake and the filter cloth, reducing filter cloth wear and keeping the alkalinity of the filter cloth at a low level, extending the service life of the filter cloth and reducing the frequency and cost of consumable replacement.

[0047] In some embodiments, the amount of the filter aid is 0.02~0.04 kg / m³. 3 The filter aid is a sulfonate copolymer.

[0048] The sulfonate copolymer has a solid content ≥20%, a pH value (10 g / L aqueous solution) of 4~8, and a density of 1.08~1.12 g / cm³ at 20°C. 3 .

[0049] In some embodiments, the temperature of the penetrating radiation heating is 85~90°C.

[0050] In some embodiments, the temperature of the wash water is 30-35°C, and the volume is 20-25 ml. 3 / h; In some embodiments, the temperature of the second-stage washing water is 40-45°C, and the dosage is 18-20 ml. 3 / h; In some embodiments, the temperature of the three-stage washing water is 40~45℃, and the dosage is 15~20 ml. 3 / h.

[0051] Preferably, the washing liquid after the three-stage washing process passes through the second-stage washing tank 58 and the second-stage washing pump 59 in sequence and enters the second-stage washing pipe 41 for secondary washing. The washing liquid after the secondary washing passes sequentially through the washing water separator 42, the first-stage washing water tank 43 and the first-stage washing water pump 44 into the first-stage washing water pipe 31 for primary washing. The washing liquid after the first wash passes through a washing water pipe 31 and a mother liquor separator 32 before entering the mother liquor tank 33. The secondary wash water and its gas phase enter the filtration tail gas ammonia purification tower 54 for treatment, and then are vented by a vacuum pump.

[0052] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and are not intended to limit the scope of protection of the present invention. Although the present invention has been described in detail with reference to preferred embodiments, those skilled in the art should understand that modifications or equivalent substitutions can be made to the technical solutions of the present invention without departing from the essence and scope of the technical solutions of the present invention.

Claims

1. A soda ash out liquor treatment system, characterized by, The system comprises a distributor and a conveying mechanism connected in sequence, and a washing water circulation system, a filter and a medium wave infrared device are arranged in sequence along the direction of conveying soda solution out of soda liquor along the conveying mechanism; The washing water circulation system comprises a first washing water mechanism, a second washing water mechanism and a third washing water mechanism arranged in sequence, the first washing water mechanism comprises a first washing water pipeline, a mother liquor separator and a mother liquor barrel connected in sequence, the second washing water pipeline comprises a second washing water pipeline, a washing water separator, a first washing water barrel and a first washing water pump connected in sequence, the first washing water pump is used to connect the first washing water barrel and the first washing water pipeline, and the third washing water mechanism comprises a vacuum machine, a multi-purpose tank, a desalted water circulating pump, a filtered tail gas ammonia removal tower, a calcined tail gas ammonia removal tower, a high tank, a third washing water pipeline, a second washing water barrel and a second washing water pump connected in sequence.

2. The soda ash out-of-ash liquor treatment system of claim 1, wherein, The system further comprises a filter aid barrel and a filter aid pump connected in sequence, and the filter aid pump is connected with the third washing water pipeline.

3. The soda ash out-of-ash liquor treatment system of claim 1, wherein, The gas outlet end of the mother liquor separator is connected with the filtered tail gas ammonia removal tower.

4. The soda ash out-of-ash liquor treatment system of claim 1, wherein, The gas outlet end of the washing water separator is connected with the filtered tail gas ammonia removal tower.

5. The soda ash out-of-ash liquor treatment system of claim 1, wherein, The high tank is further connected with the multi-purpose tank.

6. The soda ash out-of-ash liquor treatment system of claim 1, wherein, A buffer barrel is further arranged between the filtered tail gas ammonia removal tower and the calcined tail gas ammonia removal tower. A washing water pressurizing pump is further arranged between the second washing water pump and the second water supply pipeline.

7. A soda ash discharging liquid treatment method characterized by, The soda solution out of soda liquor treatment system based on any one of claims 1-6 comprises the following steps: S1: the desalted water is sent into the multi-purpose tank after being heated for the first time by the vacuum machine, and then is sent to the filtered tail gas ammonia removal tower and the calcined tail gas ammonia removal tower for the second and third heatings by the desalted water circulating pump in sequence, and the desalted water after being heated is sent into the high tank; S2: the soda solution out of soda liquor is uniformly distributed on the conveying structure by the distributor, and is sequentially subjected to the first washing, the second washing and the third washing along the movement direction of the conveying mechanism, wherein the third washing is mixed with the filter aid according to a mixing ratio to wash the heavy soda filter cake, and then is subjected to the treatment by the filter and the penetration radiation heating by the medium wave infrared device.

8. The soda ash out-of-ash liquor treatment method according to claim 7, characterized by, The filter aid is used in an amount of 0.02 to 0.04 kg / m 3 ; the filter aid is a sulfonate copolymer.

9. The soda ash out-of-ash liquor treatment method according to claim 7, characterized by, The temperature of the penetration radiation heating is 85-90℃. The temperature of the washing water is 30-35℃, and the amount is 20-25m 3 / h; The temperature of the second section washing water is 40-45℃, and the dosage is 18-20m 3 / h; The temperature of the three sections of washing water is 40-45℃, and the amount is 15-20m 3 / h.

10. The soda ash out-of-ash liquor treatment method of claim 7, wherein, The washing liquid after the third washing is sequentially sent into the second washing water pipeline through the second washing water barrel and the second washing water pump for the second washing. The washing liquid after the second washing is sequentially sent into the first washing water pipeline through the washing water separator, the first washing water barrel and the first washing water pump for the first washing. The washing liquid after the first washing is sequentially sent into the mother liquor barrel through the first washing water pipeline and the mother liquor separator. The gas phase of the second washing and the second washing is sent into the filtered tail gas ammonia removal tower for treatment, and then is discharged by the vacuum pump.

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