Ammonia washing water deamination system
By using a hydrogen sulfide tower and a deamination tower in the ammonia washing water deamination system, and using steam heating technology to efficiently remove ammonia and hydrogen sulfide in the ammonia washing water, the problem of difficulty in removing these two pollutants at the same time in the prior art is solved, and the improvement of water quality and efficient recycling of resources are achieved.
Patent Information
- Application Number
- CN202421825545.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-07-30
- Publication Date
- 2025-05-30
- Estimated Expiration
- 2034-07-30
AI Technical Summary
The prior art is difficult to efficiently remove ammonia and hydrogen sulfide in the ammonia washing water at the same time, which makes it difficult for the treated water quality to meet the emission standards, and the resource recovery rate is low, resulting in resource waste problems.
A deammonia ammonia water washing system is adopted, including a desulfurization tower and a deammonia tower. By heating low-pressure steam and medium-pressure steam, hydrogen sulfide and ammonia in the deammonia water are removed respectively to achieve efficient separation of the two.
It realizes efficient separation of ammonia and hydrogen sulfide in ammonia washing water, meets emission standards, improves resource recovery rate, and reduces resource waste.
Smart Images
Figure CN222922936U_ABST
Abstract
Description
Technical Field
[0001] This application relates to the technical field of coal chemical industry, and particularly relates to a wash ammonia water deammoniation system. Background Art
[0002] In the current chemical and environmental protection industries, semi-coke ammonia water, as a by-product, is widely generated during processes such as coal processing and coking. This ammonia water often contains high concentrations of ammonia and hydrogen sulfide. If directly discharged, it will not only cause serious environmental pollution but also waste the recyclable resources therein. Traditional treatment methods often have difficulty in efficiently removing ammonia and hydrogen sulfide in ammonia water simultaneously, resulting in the treated water quality still being difficult to meet the discharge standards, and the resource recovery rate is low during the treatment process, with a large problem of resource waste.
[0003] Existing technologies usually adopt a single deammoniation or desulfurization process, but these methods often have the disadvantage of unstable treatment effects. In addition, due to the different existence forms and reaction characteristics of ammonia and hydrogen sulfide in water, a single treatment process is difficult to effectively remove both simultaneously. Utility Model Content
[0004] The embodiment of this application provides a wash ammonia water deammoniation system, which solves the problem that the ammonia content and hydrogen sulfide content in the wash ammonia water in the prior art are high, cannot meet the discharge standards, and are prone to cause resource waste, realizes the efficient separation of ammonia and hydrogen sulfide in the wash ammonia water, and provides conditions for the subsequent recovery of hydrogen sulfide and ammonia in the process.
[0005] The embodiment of this utility model provides a wash ammonia water deammoniation system, including a hydrogen sulfide removal tower, a deammoniation tower, a raw water tank, a first bottom reboiler, and a second bottom reboiler; the input end of the raw water tank inputs semi-coke ammonia water, the first input end of the hydrogen sulfide removal tower is connected to the output end of the raw water tank, and the first output end of the hydrogen sulfide removal tower is connected to the first input end of the deammoniation tower; a low-pressure steam is introduced into the second input end of the hydrogen sulfide removal tower; the third input end of the hydrogen sulfide removal tower is connected to the first output end of the first bottom reboiler; a medium-pressure steam is introduced into the first input end of the first bottom reboiler; a low-pressure steam is introduced into the second input end of the deammoniation tower; the third input end of the deammoniation tower is connected to the first output end of the second bottom reboiler; a medium-pressure steam is introduced into the first input end of the second bottom reboiler.
[0006] In a possible implementation, it further includes a first condensate water tank and a second condensate water tank; the second output end of the hydrogen sulfide removal tower is connected to the second input end of the first bottom reboiler, the second output end of the first bottom reboiler is connected to the input end of the first condensate water tank, and the output end of the first condensate water tank outputs purified water; the first output end of the ammonia removal tower is connected to the second input end of the second bottom reboiler; the second output end of the second bottom reboiler is connected to the input end of the second condensate water tank, and the output end of the second condensate water tank outputs purified water.
[0007] In a possible implementation, it further includes a first raw material water pump, a second raw material water pump, and a third raw material water pump; the first raw material water pump is also connected between the hydrogen sulfide removal tower and the raw material water tank; the second raw material water pump is also connected between the hydrogen sulfide removal tower and the raw material water tank; the third raw material water pump is also connected between the hydrogen sulfide removal tower and the raw material water tank.
[0008] In a possible implementation, it further includes a first ammonia removal water pump, a second ammonia removal water pump, a third ammonia removal water pump, and an ammonia removal water cooler; the input end of the ammonia removal water cooler is connected to the third output end of the hydrogen sulfide removal tower, the output end of the ammonia removal water cooler is connected to one end of the first ammonia removal water pump, and the other end of the first ammonia removal water pump is connected to the fourth input end of the hydrogen sulfide removal tower; the output end of the ammonia removal water cooler is connected to one end of the second ammonia removal water pump, and the other end of the second ammonia removal water pump is connected to the fourth input end of the hydrogen sulfide removal tower; the output end of the ammonia removal water cooler is connected to one end of the third ammonia removal water pump, and the other end of the third ammonia removal water pump is connected to the fourth input end of the hydrogen sulfide removal tower.
[0009] In a possible implementation, it further includes an ammonia removal tower top reflux tank and an ammonia removal tower top circulation pump; the second output end of the ammonia removal tower is connected to the input end of the ammonia removal tower top reflux tank, the output end of the ammonia removal tower top reflux tank is connected to one end of the ammonia removal tower top circulation pump, and the other end of the ammonia removal tower top circulation pump is connected to the fourth input end of the ammonia removal tower.
[0010] One or more technical solutions provided by this application have at least the following technical effects:
[0011] An embodiment of the present utility model adopts a washing ammonia water deammoniation system, which includes a hydrogen sulfide removal tower, a deammoniation tower, a raw material water tank, a first bottom reboiler, and a second bottom reboiler; the input end of the raw material water tank inputs semi-coke ammonia water, the first input end of the hydrogen sulfide removal tower is connected to the output end of the raw material water tank, and the first output end of the hydrogen sulfide removal tower is connected to the first input end of the deammoniation tower; the raw material water tank can store semi-coke ammonia water, the hydrogen sulfide removal tower can remove hydrogen sulfide in the semi-coke ammonia water, and the deammoniation tower can remove the remaining ammonia; low-pressure steam is introduced into the second input end of the hydrogen sulfide removal tower; the third input end of the hydrogen sulfide removal tower is connected to the first output end of the first bottom reboiler; medium-pressure steam is introduced into the first input end of the first bottom reboiler; the hydrogen sulfide removal tower can receive the ammonia water from the raw material water tank and be heated by the first bottom reboiler heated by low-pressure steam and medium-pressure steam to remove hydrogen sulfide in the ammonia water; low-pressure steam is introduced into the second input end of the deammoniation tower; the third input end of the deammoniation tower is connected to the first output end of the second bottom reboiler; medium-pressure steam is introduced into the first input end of the second bottom reboiler. The deammoniation tower receives the ammonia water treated by the hydrogen sulfide removal tower and is further heated by the second bottom reboiler heated by low-pressure steam and medium-pressure steam to remove the remaining ammonia, so that the separation of hydrogen sulfide and ammonia in the semi-coke ammonia water can be realized, providing conditions for the subsequent recovery of hydrogen sulfide and ammonia respectively in the process. This application solves the problem that the ammonia content and hydrogen sulfide content in the washing ammonia water in the prior art are relatively high, cannot meet the emission standards and are prone to cause waste of resources, realizes the separation of ammonia and hydrogen sulfide in the washing ammonia water, and provides conditions for the subsequent recovery of hydrogen sulfide and ammonia respectively in the process. Description of the Drawings
[0012] In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the drawings required for the description of the embodiments of the present utility model will be briefly introduced below. Obviously, the drawings in the following description are some embodiments of the present utility model. For those of ordinary skill in the art, other drawings can be obtained based on these drawings without creative efforts.
[0013] Figure 1 It is a schematic diagram of the system of the raw material water tank provided by the embodiment of the present application;
[0014] Figure 2 It is a schematic diagram of the system of the hydrogen sulfide removal tower provided by the embodiment of the present application;
[0015] Figure 3 It is a schematic diagram of the system of the deammoniation tower provided by the embodiment of the present application.
[0016] Icons: 1 - hydrogen sulfide removal tower; 2 - ammonia removal tower; 3 - raw water tank; 4 - first bottom reboiler; 5 - second bottom reboiler; 6 - first condensate tank; 7 - second condensate tank; 8 - first raw water pump; 9 - second raw water pump; 10 - third raw water pump; 11 - first ammonia removal water pump; 12 - second ammonia removal water pump; 13 - third ammonia removal water pump; 14 - ammonia removal water cooler; 15 - ammonia removal tower top reflux tank; 16 - ammonia removal tower top circulation pump. Detailed implementation manners
[0017] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all of the embodiments. Based on the embodiments in the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention.
[0018] In the description of the embodiments of the present invention, it should be noted that the orientation or positional relationship indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. is based on the orientation or positional relationship shown in the accompanying drawings. It is only for the convenience of describing the embodiments of the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as a limitation to the present invention. The terms "first", "second", "third" are only used for descriptive purposes and cannot be construed as indicating or implying relative importance. In addition, the terms "installation", "connection", "connection" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected, or indirectly connected through an intermediate medium, and it can be the internal communication of two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the embodiments of the present invention can be understood according to specific circumstances.
[0019] An embodiment of the present utility model provides a washing ammonia water deammoniation system, which includes a hydrogen sulfide removal tower 1, a deammoniation tower 2, a raw water tank 3, a first bottom reboiler 4 and a second bottom reboiler 5; the input end of the raw water tank 3 inputs semi-coke ammonia water, the first input end of the hydrogen sulfide removal tower 1 is connected to the output end of the raw water tank 3, and the first output end of the hydrogen sulfide removal tower 1 is connected to the first input end of the deammoniation tower 2; a low-pressure steam is introduced into the second input end of the hydrogen sulfide removal tower 1; the third input end of the hydrogen sulfide removal tower 1 is connected to the first output end of the first bottom reboiler 4; a medium-pressure steam is introduced into the first input end of the first bottom reboiler 4; a low-pressure steam is introduced into the second input end of the deammoniation tower 2; the third input end of the deammoniation tower 2 is connected to the first output end of the second bottom reboiler 5; a medium-pressure steam is introduced into the first input end of the second bottom reboiler 5.
[0020] Exemplarily, the treatment of sulfur-containing and ammonia-containing acidic water by the stripping method is a process of stripping volatile hydrogen sulfide and ammonia from the acidic water by heating, purifying the acidic water, and separating and extracting ammonia and hydrogen sulfide. The acidic water stripping process is a complex system coexisting with chemistry, ionization and phase equilibrium. In this application, the separation of hydrogen sulfide and ammonia is completed by the hydrogen sulfide removal tower 1 and the deammoniation tower 2. Specifically, the main task of the hydrogen sulfide removal tower 1 is to separate hydrogen sulfide. Inside the tower, by controlling the temperature and phase equilibrium, hydrogen sulfide is transferred from the liquid phase to the gas phase and enriched at the top of the tower, achieving the technical effect that high-concentration hydrogen sulfide gas is extracted; the deammoniation tower 2 can further treat the acidic water from the bottom of the hydrogen sulfide removal tower 1, and the main purpose is to separate ammonia. Through a higher temperature and the stripping effect of multiple trays, ammonia is also transferred from the liquid phase to the gas phase and enriched at the top of the tower, while purified water is discharged from the bottom of the tower.
[0021] Exemplarily, under certain conditions, hydrogen sulfide reacts with ammonia to form ammonium bisulfide, which is a weak electrolyte and its ionization degree and chemical reactions are significantly affected by temperature. At low temperatures, ammonium bisulfide tends to remain in the liquid phase, thereby helping to fix ammonia in the liquid phase at the top of the tower and reducing the ammonia content in the gas phase. Specifically, acidic water enters from the lower part of the hydrogen sulfide removal tower 1, and steam is introduced into the hydrogen sulfide removal tower 1 through the steam inlet at the bottom or in the middle of the tower. During the contact between the steam and the acidic water, the upward flow of the steam and the downward flow of the raw liquid form a countercurrent contact, increasing the mass transfer area and mass transfer driving force between the gas and the liquid. Hydrogen sulfide and ammonia in the acidic water are desorbed due to the heating and dilution effects of the steam and rise to the top of the tower together with the steam. At the same time, part of the heat in the steam is also transferred to the raw liquid, gradually increasing its temperature. At the top of the hydrogen sulfide removal tower 1, due to the relatively low temperature (about 40 °C), ammonia tends to react with hydrogen sulfide to form ammonium bisulfide and thus remains in the liquid phase, while hydrogen sulfide exists more in the gas phase due to its lower solubility. Also, because of the large difference in the solubility of hydrogen sulfide and ammonia, when the low-temperature liquid phase at the top of the tower meets the upward gas phase at the bottom of the tower, the amount of ammonia dissolved in water in the gas phase is greater than that of hydrogen sulfide dissolved in water. When the gas phase rises to the top of the tower, the ammonia content in the gas phase is very low, while the hydrogen sulfide content is relatively high. Therefore, under the relatively low temperature conditions at the top of the tower, ammonia can be fixed in the liquid phase in the form of ammonium bisulfide, reducing the ammonia in the gas phase drawn from the top of the hydrogen sulfide removal tower 1 to a very low level, while the hydrogen sulfide content can reach more than 90%.
[0022] Exemplarily, temperature is a key factor in the stripping process. In the ammonia stripping tower 2, by controlling the temperature in different regions, the separation effect of hydrogen sulfide and ammonia can be optimized. High temperature helps to promote the transfer of hydrogen sulfide and ammonia from the liquid phase to the gas phase, thus achieving a more thorough separation. Specifically, in the upper-middle part of the ammonia stripping tower 2, the hot feed temperature reaches about 140 °C. In this state, salts formed by a small amount of hydrogen sulfide and ammonia have decomposed into free molecular states. After entering the tower, a small amount of hydrogen sulfide and ammonia are transferred from the liquid phase to the gas phase. Stripping steam with a relatively high temperature is introduced at the bottom of the ammonia stripping tower 2 to make the bottom temperature of the tower reach about 160 °C. At this temperature, ammonia and a small amount of hydrogen sulfide in the liquid phase exist completely in the form of free molecules. Under the action of the relatively high temperature and multi-layer trays in the lower part of the ammonia stripping tower 2, ammonia and hydrogen sulfide that are difficult to decompose in water are more thoroughly separated and transferred to the gas phase. The purified water discharged from the bottom of the tower contains very little ammonia and hydrogen sulfide.
[0023] Exemplarily, cold feed is used at the top of the tower to absorb the rising ammonia and reduce the ammonia content in the gas phase. While stripping steam is introduced at the bottom of the tower to increase the bottom temperature and promote the stripping of ammonia and hydrogen sulfide.
[0024] In the embodiment of the present application, a first condensate tank 6 and a second condensate tank 7 are further included; the second output end of the hydrogen sulfide removal tower 1 is connected to the second input end of the first bottom reboiler 4, the second output end of the first bottom reboiler 4 is connected to the input end of the first condensate tank 6, and the output end of the first condensate tank 6 outputs purified water; the first output end of the ammonia removal tower 2 is connected to the second input end of the second bottom reboiler 5; the second output end of the second bottom reboiler 5 is connected to the input end of the second condensate tank 7, and the output end of the second condensate tank 7 outputs purified water.
[0025] Exemplarily, the first condensate tank 6 is mainly used to collect the condensate generated by the bottom reboiler of the hydrogen sulfide removal tower 1. During the hydrogen sulfide removal process, these condensates are heated by medium-pressure steam, part of the water evaporates, and the remaining condensates are processed and then output as purified water. This process not only removes hydrogen sulfide from the water but also improves the purity of the water. The processed purified water is discharged from the output end of the first condensate tank 6 for subsequent processes or emissions.
[0026] Exemplarily, the second condensate tank 7 is used to collect the condensate generated by the bottom reboiler of the ammonia removal tower 2. During the ammonia removal process, these condensates are heated at high temperature and subjected to stripping to remove ammonia and other impurities, and finally output as purified water. The processed purified water is discharged from the output end of the second condensate tank 7 for subsequent processes or emissions.
[0027] In the embodiment of the present application, a first raw material water pump 8, a second raw material water pump 9, and a third raw material water pump 10 are further included; a first raw material water pump 8 is also connected between the hydrogen sulfide removal tower 1 and the raw material water tank 3; a second raw material water pump 9 is also connected between the hydrogen sulfide removal tower 1 and the raw material water tank 3; a third raw material water pump 10 is also connected between the hydrogen sulfide removal tower 1 and the raw material water tank 3.
[0028] Exemplarily, the first raw material water pump 8, the second raw material water pump 9, and the third raw material water pump 10 can all transport the semi-coke ammonia water in the raw material water tank 3 to the hydrogen sulfide removal tower 1. Among them, the flow rates of the first raw material water pump 8 and the second raw material water pump 9 are 30 cubic meters per hour, and the head is 90 meters; the flow rate of the third raw material water pump 10 is 40 cubic meters per hour, and the head is 120 meters. Under low-load operating conditions, the first raw material water pump 8 or the second raw material water pump 9 is operated, and under high-load operating conditions, the third raw material water pump 10 is operated. Through the action of the pump, it can ensure that the semi-coke ammonia water enters the hydrogen sulfide removal tower 1 with a stable flow rate and pressure, thus ensuring the continuous operation of the entire system.
[0029] In the embodiment of the present application, it further includes a first deammoniation water pump 11, a second deammoniation water pump 12, a third deammoniation water pump 13, and a deammoniation water cooler 14; the input end of the deammoniation water cooler 14 is connected to the third output end of the hydrogen sulfide removal tower 1, the output end of the deammoniation water cooler 14 is connected to one end of the first deammoniation water pump 11, and the other end of the first deammoniation water pump 11 is connected to the fourth input end of the hydrogen sulfide removal tower 1; the output end of the deammoniation water cooler 14 is connected to one end of the second deammoniation water pump 12, and the other end of the second deammoniation water pump 12 is connected to the fourth input end of the hydrogen sulfide removal tower 1; the output end of the deammoniation water cooler 14 is connected to one end of the third deammoniation water pump 13, and the other end of the third deammoniation water pump 13 is connected to the fourth input end of the hydrogen sulfide removal tower 1.
[0030] Exemplarily, the first deammoniation water pump 11, the second deammoniation water pump 12, and the third deammoniation water pump 13 can transport the deammoniation water cooled by the deammoniation water cooler 14 to the fourth input end of the hydrogen sulfide removal tower 1 for recycling or further treatment. Among them, the flow rates of the first deammoniation water pump 11, the second deammoniation water pump 12, and the third deammoniation water pump 13 are all 40 cubic meters per hour, and the head is 40 meters. Under high-load operating conditions, two of them are started, and under low-load operating conditions, only one of them needs to be started.
[0031] In the embodiment of the present application, it further includes a deammoniation tower top reflux tank 15 and a deammoniation tower top circulation pump 16; the second output end of the deammoniation tower 2 is connected to the input end of the deammoniation tower top reflux tank 15, the output end of the deammoniation tower top reflux tank 15 is connected to one end of the deammoniation tower top circulation pump 16, and the other end of the deammoniation tower top circulation pump 16 is connected to the fourth input end of the deammoniation tower 2.
[0032] Exemplarily, the rich ammonia gas extracted from the top of the deammoniation tower 2 is further processed by the principle of "high-temperature dehydration and low-temperature sulfur fixation". That is, the moisture in the gas phase is effectively reduced, and hydrogen sulfide is fixed at low temperature, thereby improving the purity and recovery efficiency of ammonia. Then, by using the step-by-step temperature reduction and pressure reduction of the partial condenser, the condensed liquid returns to the top of the tower to absorb part of the hydrogen sulfide in the gas phase, improving the purity of the gaseous ammonia. Finally, this part of the rich ammonia gas is sent to the ammonia refining section for subsequent treatment.
[0033] The various embodiments in this specification are described in a progressive manner. For the same or similar parts between the various embodiments, reference can be made to each other. The key points of each embodiment are the differences from other embodiments.
[0034] The above embodiments are only used to illustrate the technical solutions of the present application, rather than limiting the present application; although the present application has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that they can still modify the technical solutions described in the foregoing embodiments, or perform equivalent replacements on some or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the present application.
Claims
1. A system for deammoniation of ammonia washing water, characterized in that: It comprises a hydrogen sulfide removal tower (1), an ammonia removal tower (2), a raw water tank (3), a first tower bottom reboiler (4) and a second tower bottom reboiler (5); The input end of the raw water tank (3) inputs blue carbon ammonia water, the first input end of the hydrogen sulfide removal tower (1) is connected to the output end of the raw water tank (3), and the first output end of the hydrogen sulfide removal tower (1) is connected to the first input end of the deammoniation tower (2); Low-pressure steam is introduced into the second input end of the dehydrogen sulfide tower (1); The third input end of the dehydrogen sulfide tower (1) is connected to the first output end of the first tower bottom reboiler (4); medium-pressure steam is introduced into the first input end of the first tower bottom reboiler (4); Low-pressure steam is introduced into the second input end of the deamination tower (2); The third input end of the deamination tower (2) is connected to the first output end of the second tower bottom reboiler (5); and medium-pressure steam is introduced into the first input end of the second tower bottom reboiler (5).
2. The ammonia washing water deammoniation system according to claim 1, characterized in that: It also includes a first condensate tank (6) and a second condensate tank (7); The second output end of the dehydrogen sulfide tower (1) is connected to the second input end of the first tower bottom reboiler (4), the second output end of the first tower bottom reboiler (4) is connected to the input end of the first condensate tank (6), and the output end of the first condensate tank (6) outputs purified water; The first output end of the deamination tower (2) is connected to the second input end of the second tower bottom reboiler (5); the second output end of the second tower bottom reboiler (5) is connected to the input end of the second condensate tank (7), and the output end of the second condensate tank (7) outputs purified water.
3. The ammonia washing water deammoniation system according to claim 1, characterized in that: It also includes a first raw material water pump (8), a second raw material water pump (9) and a third raw material water pump (10); The first raw water pump (8) is also connected between the dehydrogen sulfide tower (1) and the raw water tank (3); The second raw water pump (9) is also connected between the dehydrogen sulfide tower (1) and the raw water tank (3); The third raw water pump (10) is also connected between the dehydrogen sulfide tower (1) and the raw water tank (3).
4. The ammonia washing water deammoniation system according to claim 1, characterized in that: It also includes a first deammoniation water pump (11), a second deammoniation water pump (12), a third deammoniation water pump (13) and a deammoniation water cooler (14); The input end of the deammoniation water cooler (14) is connected to the third output end of the deammoniation water tower (1), the output end of the deammoniation water cooler (14) is connected to one end of the first deammoniation water pump (11), and the other end of the first deammoniation water pump (11) is connected to the fourth input end of the deammoniation water tower (1); The output end of the deammoniation water cooler (14) is connected to one end of the second deammoniation water pump (12), and the other end of the second deammoniation water pump (12) is connected to the fourth input end of the dehydrogen sulfide tower (1); The output end of the deammoniation water cooler (14) is connected to one end of the third deammoniation water pump (13), and the other end of the third deammoniation water pump (13) is connected to the fourth input end of the dehydrogen sulfide tower (1).
5. The ammonia washing water deammoniation system according to claim 1, characterized in that: It also includes a deamination tower top reflux tank (15) and a deamination tower top circulation pump (16); The second output end of the deamination tower (2) is connected to the input end of the deamination tower top reflux tank (15), the output end of the deamination tower top reflux tank (15) is connected to one end of the deamination tower top circulation pump (16), and the other end of the deamination tower top circulation pump (16) is connected to the fourth input end of the deamination tower (2).