Carbonation post-treatment process for the production of soda ash by the ammonia-soda process

Abstract

The present application relates to soda ash technical field, provide a kind of for soda ash production by ammonia soda process carbonization post-treatment process, the carbonization post-treatment process includes filtration process, the mother liquor obtained by filtration process is obtained waste light liquid by mother liquor distillation system, waste light liquid is used as washing water in filtration process to produce soda ash;Mother liquor distillation system includes: ammonia tower, with first gas outlet and liquid inlet;Condenser includes multiple heat exchange boxes, multiple heat exchange boxes are stacked in the top of ammonia tower, each heat exchange box has first shell side and first tube side, multiple first shell sides are sequentially communicated, and are communicated with first gas outlet, multiple first tube sides are sequentially communicated, and are communicated with liquid inlet, the first tube side in the uppermost is used to pass into mother liquor;Gas component produced in ammonia tower exchanges heat with mother liquor, so that gas component is partially condensed into liquid A, liquid A enters ammonia tower through first gas outlet. By optimizing carbonization post-treatment process, reduce the consumption of ammonia, ensure the quality of soda ash.

Description

Technical Field

[0001] This invention relates to the field of soda ash technology, and to a carbonation post-treatment process for the production of soda ash using the ammonia-soda process. Background Technology

[0002] In the ammonia-soda process for producing soda ash, after carbonation, a filtration process is required. The mother liquor obtained from the filtration process contains ammonium chloride, sodium chloride, sodium bicarbonate, ammonium bicarbonate, ammonium sulfate, and ammonium carbonate. To recover ammonia from the mother liquor, the ammonia-soda process is currently used for ammonia stripping. The main principle is to add lime slurry to the mother liquor to react with ammonium chloride to produce ammonia. This process is often carried out in a low-resistance, sieve-reducing ammonia stripping tower under negative pressure. However, this method commonly suffers from mother liquor entrainment at the top of the tower, and the ammonia stripping load increases with the tower's capacity to reach 170 m³ / h. 3 When the flow rate exceeds a certain threshold ( / h), the entrainment situation deteriorates drastically. Summary of the Invention

[0003] Studies have found that the gas exiting the top of the ammonia stripping tower carries mother liquor, which enters the desalination tower along with the condensate. Since the desalination tower can only distill free ammonia, the fixed ammonia in the condensate, such as ammonium chloride and ammonium sulfate, will be discharged with the waste desalination, thus increasing ammonia consumption. At the same time, when this high-salt waste desalination continues to be recycled and used as washing water in the filtration process after the carbonization reaction (also known as filtration washing water), its salt content is high and fluctuates greatly, which can easily lead to excessive salt content in light ash, directly affecting the quality of soda ash products.

[0004] Based on this, the present invention provides a carbonation process for the production of soda ash using the ammonia-soda process, in order to at least partially solve the above-mentioned technical problems.

[0005] This invention provides a carbonation post-treatment process for the production of soda ash using the ammonia-soda process. The carbonation post-treatment process includes a filtration step, in which the mother liquor obtained from the filtration step at 28°C to 31°C is distilled through a mother liquor distillation system to obtain condensate. The condensate is sent to a distillation tower to generate waste distillate, which is used as washing water in the filtration step for the production of soda ash. The mother liquor contains a first component, which includes ammonium salts that react with lime milk to release ammonia gas; the first component includes ammonium chloride, ammonium sulfate, etc. The mother liquor distillation system includes: The ammonia stripping tower is equipped with a first gas outlet and a liquid inlet; the ammonia stripping tower is used to react the mother liquor with the lime slurry to produce a gaseous component containing ammonia. The condenser includes multiple heat exchange boxes stacked on top of the ammonia stripping tower. Each heat exchange box has a first shell side and a first tube side. The multiple first shell sides are connected in sequence and connected to the first gas outlet. The multiple first tube sides are connected in sequence and connected to the liquid inlet. The uppermost first tube side is used to introduce the mother liquor. The gaseous components generated in the ammonia stripping tower exchange heat with the mother liquor, causing the gaseous components to partially condense into liquid A. Liquid A then enters the ammonia stripping tower through the first gas outlet.

[0006] In the post-treatment system of the present invention, the ammonia stripping tower is the core component. The temperature of the gas components flowing through the first outlet of the ammonia stripping tower directly affects the energy consumption. Temperature control is the key to the entire post-treatment and the basis for its operation. In some specific embodiments of the present invention, the temperature of the gas components flowing through the first outlet of the ammonia stripping tower is 80°C to 82°C. Within this range, the energy consumption of the post-treatment system can be controlled within a low and reasonable range.

[0007] In some specific embodiments of the present invention, each of the heat exchange boxes includes: A box, multiple boxes are stacked on top of the ammonia stripping tower and the multiple boxes are connected. The bottommost box is connected to the first gas outlet. The space inside the box is configured as the first shell side. The heat exchange tubes are independently arranged in the multiple boxes, and the multiple heat exchange tubes are connected in sequence. The uppermost heat exchange tube is used to introduce the mother liquor, and the lowermost heat exchange tube is connected to the liquid inlet. The space inside the heat exchange tube is configured as the first tube pass.

[0008] Research has found that the heat exchange tube wall serves as both the heat exchange interface and the fluid contact interface. Compared to a vertical heat exchange device, the horizontal heat exchange device used in this invention is more conducive to condensing the gas components into liquid A, which flows into the ammonia stripping tower, reducing the amount of mother liquor carried out and reducing ammonia consumption.

[0009] In some specific embodiments of the present invention, the mother liquor contains free ammonia, which includes ammonium bicarbonate and / or ammonium carbonate; the mother liquor distillation system further includes a gas-liquid separator, and any two adjacent heat exchange tubes between the uppermost heat exchange tube and the lowermost heat exchange tube are connected through the gas-liquid separator; some of the free ammonia in the liquid B entering the gas-liquid separator undergoes a thermal decomposition reaction in the gas-liquid separator.

[0010] Studies have found that by adding the gas-liquid separator, the total amount of gas at the top of the ammonia stripping tower can be reduced, the gas velocity can be lowered, and thus the amount of mother liquor carried out can be reduced.

[0011] As described above, in the reaction system of the present invention, the temperature of the gas component at the first outlet is determined based on the energy consumption of the ammonia stripping tower and is in a basically stable state. If the temperature of the gas-liquid separator is too high, it will be detrimental to the heat exchange between the liquid C flowing out of the gas-liquid separator and the gas component at the top of the ammonia stripping tower, thereby reducing energy consumption. The upper limit of the temperature of the gas-liquid separator is the temperature value of the liquid C flowing out of the gas-liquid separator. This temperature value can be adjusted according to the required efficiency of heat exchange between the liquid C and the gas component at the top of the ammonia stripping tower. Generally, the upper limit of the temperature of the gas-liquid separator can be set to 68°C.

[0012] In this invention, the gas-liquid separator serves as a component for the thermal decomposition reaction of some of the free ammonia in liquid B. Its lower limit temperature must be at least higher than the minimum temperature at which the free ammonia in liquid B decomposes to produce gas. However, according to experiments, if the temperature is only set to the minimum temperature at which the free ammonia decomposes to produce gas, the thermal decomposition efficiency is limited, which is detrimental to the energy consumption control of the entire post-treatment system. Therefore, in some specific embodiments of this invention, the lower limit temperature of the gas-liquid separator is 65°C.

[0013] In this invention, the extended working time of the condenser can cause scale or crystallization on the surface of various components of the condenser, resulting in a decrease in cooling effect. This invention can improve the efficiency of free ammonia decomposition (especially the production of carbon dioxide) by increasing the outlet temperature of the ammonia stripping tower, reducing the amount of mother liquor entering the condenser, or strictly controlling the temperature of the mother liquor in the separator within the range of 66~68°C, which can avoid the decrease in cooling effect to a certain extent.

[0014] In some specific embodiments of the present invention, it further includes: The first pipeline, the condenser is provided with a second gas outlet, the second gas outlet is connected to the first shell side and the first pipeline, the gas-liquid separator is provided with a third gas outlet, the third gas outlet is connected to the first pipeline; The cooler is provided with an air inlet and a liquid outlet, and the air inlet is connected to the first pipeline; The second pipeline, the first end of which is connected to the liquid outlet; A collection bucket, connected to the second end of the second pipeline, is used to collect the waste desalination liquid.

[0015] In some specific embodiments of the present invention, the temperature of the gas components discharged from the second outlet is 68°C to 75°C.

[0016] In some specific embodiments of the present invention, the number of ammonia stripping towers is one or more; In some specific embodiments of the present invention, the ammonia stripping load of a single ammonia stripping tower is greater than or equal to 170m³. 3 / h.

[0017] Studies have found that the method of this invention can achieve a condensate generation rate of 6.5m³. 3 At speeds above [a certain value], the gas volume reduction reaches 10224 Nm³. 3 With a gas reduction rate of over / h, the single-tower gas reduction reaches 5112 Nm³. 3 / h or more. The condensate generation rate refers to the amount of gas components generated in the ammonia stripping tower that partially condense into liquid A due to heat exchange with the mother liquor. This condensate generation rate indicates that the mother liquor distillation system of this invention has a certain ability to wash rising gas. The gas volume reduction rate refers to the portion of the gas volume reduced in the ammonia stripping tower. The single-tower gas reduction rate refers to the reduction in gas generated at the first outlet of the ammonia stripping tower.

[0018] When the number of ammonia stripping towers is 2, the ammonia stripping towers are connected in parallel.

[0019] In some specific embodiments of the present invention, the mother liquor contains 65-72 tt of fixed ammonia and 21-26 tt of free ammonia; 40-45 tt of carbon dioxide and Cl... - Content greater than 88tt.

[0020] In this invention, the fixed ammonia includes ammonium chloride and ammonium sulfate, and the free ammonia includes ammonium bicarbonate, ammonium carbonate, NH4OH, and NH3.

[0021] In some specific embodiments of the present invention, the salt content in the waste desalination liquid is less than 0.3 tt, the ammonia content is less than 0.1 tt, and the Cl content is less than 0.3 tt. - The content is less than 0.26tt.

[0022] The desalination tower is a specialized device used for steam distillation of ammonia condensate and calcination furnace gas condensate. The resulting waste desalination liquid is used to filter and wash heavy soda ash. Because the sodium chloride content of the superior grade of light soda ash is less than 0.7%, the Cl- content of the filtered wash water is relatively low. - <0.3tt. And the Cl in the waste desalination liquid... - It mainly depends on the salt content of the condensate. In a conventional scheme, with an evaporation rate of 175m³... 3 At a rate of [amount] / h, the salinity of the condensate ranges from 1.25 to 4.6 tt, with significant fluctuations. This is the root cause of high ammonia consumption and high salinity in the waste distillate. The method described in this invention significantly reduces the entrainment of the mother liquor at the top of the column, ensuring stable salinity in the waste distillate; the ammonia content in the waste distillate is less than 0.1 tt, meeting the design requirements. [Waste distillate Cl] - The concentration decreased from 0.64tt to 0.26tt, indicating stable quality of the light gray product.

[0023] This invention provides a carbonation post-treatment process for the production of soda ash using the ammonia-soda process. On the one hand, by adding a condenser, the condensate is formed during the heat exchange with the mother liquor to wash the mother liquor carried by the rising gas, so that the waste desalinated liquid can meet the requirements of filtration washing water. On the other hand, by strictly controlling the temperature of the hot mother liquor coming out of the condenser, the decomposition of NH4HCO3 and (NH4)2CO3 is accelerated, and the released gas is reduced and sent out of the tower, thereby reducing the total amount of gas at the top of the tower and the gas velocity inside the tower, which plays a key role in reducing the amount of mother liquor carried by the gas. Attached Figure Description

[0024] To more clearly illustrate the technical solutions in this invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0025] Figure 1 This is one of the structural schematic diagrams of the mother liquor distillation system for soda ash production provided by the present invention.

[0026] Figure label: 10. Ammonia stripping tower; 101. Liquid inlet; 20. Condenser; 21. First chamber; 22. Second chamber; 23. Third chamber; 24. Fourth chamber; 201. Second gas outlet; 30. Gas-liquid separator; 301. Third gas outlet; 40. Cooler; 41. Cooling tank; 50. Collection tank; 60. Pump; 81. First pipeline; 82. Second pipeline; 84. Fourth pipeline; 85. Fifth pipeline; 86. Sixth pipeline; 87. Seventh pipeline; 88. Eighth pipeline; 89. Ninth pipeline. Detailed Implementation

[0027] To make the objectives, technical solutions, and advantages of this invention clearer, the technical solutions of this invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0028] Equipment Example 1 like Figure 1 As shown, a mother liquor distillation system comprises: two parallel ammonia stripping tower systems, a cooler 40, a collection tank 50, several third pipelines, several regulating valves, several flow meters, several first temperature sensors, several second temperature sensors, and several third temperature sensors connected to the ammonia stripping tower systems.

[0029] One ammonia stripping tower system consists of one ammonia stripping tower 10, one condenser 20, and one gas-liquid separator 30. The connection relationship between the ammonia stripping tower 10, condenser 20, and gas-liquid separator 30 in this ammonia stripping tower system is as follows: The ammonia stripping tower 10 is equipped with a first gas outlet and a liquid inlet 101.

[0030] The condenser 20 includes four heat exchange boxes stacked in sequence. The two middle heat exchange boxes are connected through a gas-liquid separator 30. The bottom box is connected to the ammonia stripping tower 10 and to the first gas outlet. The space inside the box is configured as the first shell side. Heat exchange tubes are installed inside the box. The four heat exchange tubes are connected in sequence. The top heat exchange tube is used to introduce mother liquor. The bottom heat exchange tube is connected to the liquid inlet 101. The space inside the heat exchange tube is configured as the first tube side.

[0031] Specifically, the four chambers are arranged from bottom to top as follows: chamber 21, chamber 22, chamber 23, and chamber 24. The diameter of each chamber is equal to the diameter of the ammonia stripping tower 10. Chamber 21 is connected to the top flange of the ammonia stripping tower 10 and is also connected to the first gas outlet. The gas components flow sequentially from the first gas outlet through chambers 21, 22, 23, and 24. Chamber 21 contains a first heat exchange tube, chamber 22 contains a second heat exchange tube, chamber 23 contains a third heat exchange tube, and chamber 24 contains a fourth heat exchange tube. The inlet of the fourth heat exchange tube is connected to a ninth pipe 89, which is used to introduce the mother liquor. The outlet of the fourth heat exchange tube is connected to the inlet of the third heat exchange tube. The outlet of the third heat exchange tube is connected to the inlet of the gas-liquid separator 30 via the fourth pipe 84. The outlet of the gas-liquid separator 30 is connected to the inlet of the second heat exchange tube via the fifth pipe 85. The outlet of the second heat exchange tube is connected to the inlet of the first heat exchange tube. The outlet of the first heat exchange tube is connected to the inlet 101 of the ammonia stripping tower 10 via the sixth pipe 86. In general, the mother liquor flows from the uppermost first tube side to the lowermost first tube side, and finally enters the ammonia stripping tower 10 through the inlet 101.

[0032] The mother liquor in the ammonia stripping tower 10 is mixed with lime slurry and heated and distilled within the tower. The resulting gaseous components flow sequentially through each of the first shell sides from bottom to top through the first outlet. During the flow, the gaseous components exchange heat with the mother liquor. Some of the water vapor in the gaseous components shrinks in volume and condenses into condensate. As the condensate flows downward, it counter-washes the rising gaseous components, causing some of the mother liquor carried in the gaseous components to detach and enter the ammonia stripping tower 10 through the first outlet, thereby reducing the amount of mother liquor entrained in the gas exiting the top of the ammonia stripping tower 10.

[0033] The two heat exchange tubes in the middle are connected by a gas-liquid separator 30. When the mother liquor flows through the fourth and third heat exchange tubes, it exchanges heat with the gas components, and the temperature of the mother liquor rises. The heated mother liquor enters the gas-liquid separator 30 for gas-liquid separation. Some of the free ammonia in the liquid entering the gas-liquid separator undergoes a thermal decomposition reaction in the gas-liquid separator. The separated liquid enters the second heat exchange tube, and then flows through the first heat exchange tube, where it exchanges heat with the gas components again.

[0034] The condenser 20 is provided with a second outlet 201. After the gas components exchange heat with the mother liquor in the first shell side, they enter the first pipeline 81 through the second outlet 201. The gas-liquid separator 30 is provided with a third outlet 301. The gas components separated in the gas-liquid separator 30 enter the first pipeline 81 through the third outlet 301. The cooler 40 is provided with an inlet and a outlet. The gas components in the first pipeline 81 enter the cooler 40 through the inlet. The water vapor in the gas components is condensed into liquid in the cooler 40. The liquid enters the collection tank 50 through the outlet and the second pipeline 82 for collection.

[0035] The cooler 40 includes multiple cooling boxes 41, which are stacked sequentially. Each cooling box 41 has a second shell side and a second tube side, with the multiple second shell sides and tube sides connected sequentially. The lowermost second shell side is connected to the first pipe 81 and the second pipe 82, the uppermost second tube side is used to introduce the cooling medium through the seventh pipe 87, and the lowermost second tube side is used to discharge the cooling medium through the eighth pipe 88.

[0036] Specifically, the gaseous components that enter the cooler 40 through the first pipe 81 flow in the second shell side, with the flow path from bottom to top; the cooling medium flows in the second tube side, with the flow path from top to bottom. The two exchange heat fully during the flow process, and the condensed liquid falls into the lowest second shell side and enters the collection tank 50 through the second pipe 82.

[0037] A pump 60 is installed on the second pipeline 82 to pump the condensed liquid into the collection tank 50.

[0038] The cooler 40 is provided with a fourth air outlet, through which the gas that has not been condensed into liquid is discharged from the cooler 40.

[0039] The third pipeline is connected to the ammonia stripping tower 10 and is used to introduce steam into the ammonia stripping tower 10. A regulating valve and a flow meter are installed on the third pipeline. The regulating valve is used to regulate the flow rate of steam in the third pipeline, and the flow meter is used to detect the flow rate of steam in the third pipeline.

[0040] A first temperature sensor is disposed at the first outlet and is used to detect the temperature of the gas components flowing through the first outlet; a second temperature sensor is disposed at the second outlet 201 and is used to detect the temperature of the gas components flowing through the second outlet 201; a third temperature sensor is disposed at the third outlet 301 and is used to detect the temperature of the gas components flowing through the third outlet 301.

[0041] Example 1 A carbonation post-treatment process for the production of soda ash using the ammonia-soda process involves treating the mother liquor obtained at 30°C from the filtration process through the mother liquor distillation system in the aforementioned equipment example 1 to obtain condensate. The condensate is then sent to a distillation tower to generate waste distillate, which is then used as washing water in the aforementioned filtration process to continue producing soda ash.

[0042] The mother liquor contained 65-72 tt of fixed ammonia and 21-26 tt of free ammonia; 40-45 tt of carbon dioxide and Cl... - Content greater than 88tt; The temperature of the gas components flowing through the first outlet of the ammonia stripping tower is 80℃.

[0043] The temperature of the gas-liquid separator is 65~68℃.

[0044] The temperature of the gas components discharged from the second outlet is 68℃~75℃.

[0045] The ammonia stripping load of a single ammonia stripping tower is 179m³. 3 / h, the total steaming capacity of the two ammonia stripping towers is 358m³. 3 / h.

[0046] Tests revealed that the salt content in the waste desalination liquid was less than 0.3 tt, the ammonia content was less than 0.1 tt, and the Cl content was... - With a content of less than 0.26tt, the quality of the light ash product is stable, and the ammonia consumption of this production line is 0.035~0.069kg / t alkali.

[0047] Comparative Example 1 This is essentially the same as Example 1, except that the mother liquor distillation system in Example 1 is replaced with a mother liquor distillation system that does not contain a condenser and a gas-liquid separator. Testing revealed that the waste desalination liquid contained Cl... - The content is 0.64tt, and the ammonia consumption of this production line is 0.30~0.38kg / t.

[0048] Monitoring data revealed that the condensate generation rate of the liquid distillation system in Example 1 was approximately 6.5 m³. 3 / h, the gas volume decrease is approximately 10224 Nm 3 / h, the gas reduction per tower is approximately 5112 Nm³. 3 / h.

[0049] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A carbonization post-treatment process for the production of soda ash using the ammonia-soda process, the carbonization post-treatment process including a filtration step, characterized in that, The mother liquor obtained from the filtration process at 28℃~31℃ is passed through a mother liquor distillation system to obtain condensate. The condensate is sent to a distillation tower to generate waste distillate, which is used as washing water in the filtration process to produce soda ash. The mother liquor contains fixed ammonia; The mother liquor distillation system includes: The ammonia stripping tower is equipped with a first gas outlet and a liquid inlet. The condenser includes multiple heat exchange boxes stacked on top of the ammonia stripping tower. Each heat exchange box has a first shell side and a first tube side. The multiple first shell sides are connected in sequence and connected to the first gas outlet. The multiple first tube sides are connected in sequence and connected to the liquid inlet. The uppermost first tube side is used to introduce the mother liquor. The gaseous components generated in the ammonia stripping tower exchange heat with the mother liquor, causing the gaseous components to partially condense into liquid A. Liquid A then enters the ammonia stripping tower through the first gas outlet.

2. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to claim 1, characterized in that, The temperature of the gas components flowing through the first outlet of the ammonia stripping tower is 80℃~82℃.

3. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to claim 1 or 2, characterized in that, Each of the heat exchange boxes includes: A box, multiple boxes are stacked on top of the ammonia stripping tower and the multiple boxes are connected. The bottommost box is connected to the first gas outlet. The space inside the box is configured as the first shell side. Heat exchange tubes are installed inside the box, and multiple heat exchange tubes are connected in sequence. The uppermost heat exchange tube is used to introduce the mother liquor, and the lowermost heat exchange tube is connected to the liquid inlet. The space inside the heat exchange tubes is configured as the first tube pass.

4. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to claim 3, characterized in that, The mother liquor contains free ammonia, which includes ammonium bicarbonate and / or ammonium carbonate; the mother liquor distillation system also includes a gas-liquid separator, and any two adjacent heat exchange tubes between the uppermost and lowermost heat exchange tubes are connected through the gas-liquid separator; some of the free ammonia in the liquid B entering the gas-liquid separator undergoes a thermal decomposition reaction in the gas-liquid separator.

5. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to claim 4, characterized in that, The temperature of the gas-liquid separator is greater than or equal to 65°C.

6. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to claim 4 or 5, characterized in that, Also includes: The first pipeline, the condenser is provided with a second gas outlet, the second gas outlet is connected to the first shell side and the first pipeline, the gas-liquid separator is provided with a third gas outlet, the third gas outlet is connected to the first pipeline; The cooler is provided with an air inlet and a liquid outlet, and the air inlet is connected to the first pipeline; The second pipeline, the first end of which is connected to the liquid outlet; A collection bucket, connected to the second end of the second pipeline, is used to collect the waste desalination liquid.

7. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to claim 6, characterized in that, The temperature of the gas components discharged from the second outlet is 68℃~75℃.

8. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to claim 1, characterized in that, The number of ammonia stripping towers is one or more; Preferably, the ammonia stripping load of a single ammonia stripping tower is greater than or equal to 170m³. 3 / h.

9. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to any one of claims 1 to 8, characterized in that, The mother liquor contains 65-72 tt of fixed ammonia and 21-26 tt of free ammonia; 40-45 tt of carbon dioxide and Cl... - Content greater than 88tt.

10. The carbonization post-treatment process for producing soda ash using the ammonia-soda process according to any one of claims 1 to 9, characterized in that, The waste desalinated liquid contains less than 0.3 tt of salt, less than 0.1 tt of ammonia, and less than 0.3 tt of Cl. - The content is less than 0.26tt.

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