Ammonia distillation device and method for improving operation quality of ammonia distillation process

Abstract

The invention relates to the field of ammonia distillation process production, in particular to an ammonia distillation device and a method for improving the operation quality of the ammonia distillation process, the ammonia distillation device comprises an ammonia distillation tower, an ammonia distillation tube furnace, an ammonia dephlegmator, a condensation cooler, a reaction tower, a concentrated ammonia water tank, an adsorption tower and a residual ammonia water heat exchanger; the ammonia gas stripping and rectifying process in the tower is changed into the following gas-liquid mass transfer process: an acid gas rectifying section between the top and a hot feeding plate, an acid gas stripping section between the hot feeding plate and a side line extraction plate, an ammonia stripping section between a side line outlet and the tower bottom, ammonia distillation wastewater flowing out of the tower bottom, acid gas extracted from the tower top and ammonia gas extracted from the side line, and introducing the condensed ammonia gas into an adsorption tower, and carrying out adsorption treatment by the adsorption tower to obtain high-quality stronger ammonia water. According to the method, the content of sulfide and cyanide in the ammonia distillation wastewater is reduced, the corrosion condition of equipment in the process is reduced, the naphthalene and oil content of the delivered stronger ammonia water is reduced, and the mass concentration of the delivered stronger ammonia water and the economic benefit of the product are improved.

Description

Technical Field

[0001] The invention relates to the technical field of ammonia distillation process production, and in particular to an ammonia distillation device and a method for improving the operation quality of the ammonia distillation process. Background Art

[0002] The ammonia distillation process distills the remaining ammonia water from the blast condensation section. The ammonia gas produced at the top of the ammonia distillation tower is cooled to obtain concentrated ammonia water as an export product. The ammonia distillation wastewater obtained at the bottom of the tower is sent to the wastewater treatment unit for deamination and decarbonization. The following problems occurred in the actual operation of the process: (1) The naphthalene content in the coal gas, tar, and ammonia water produced by the coking chemical industry is generally high. Naphthalene exists as a light component in the remaining ammonia water. During the ammonia distillation process, it enters the reducer together with the ammonia gas, and is mixed into the concentrated ammonia water after condensation and cooling. Since the concentrated ammonia water contains impurities such as naphthalene, it is easy to cause pipeline blockage. In addition, the concentration of the concentrated ammonia water is about 14%, and the quality of the concentrated ammonia water is poor, which affects the export of the product and the economic benefits; (2) After the system is put into use, due to the presence of S in the concentrated ammonia water, the concentrated ammonia water 2- , HS - 、CO3 2- , HCO 3- , etc., resulting in frequent corrosion, leakage and blockage of pipelines and equipment from the ammonia condenser cooler to the adsorption tower; (3) The cyanide and sulfide content in the wastewater is relatively high, affecting the stable operation of the back-end biochemical process.

[0003] As the main process for treating residual ammonia water, the ammonia distillation process often faces the problems of poor quality of concentrated ammonia water for export, serious corrosion of equipment in the process, prominent foam dripping, and heavy odor. In addition, the concentrated ammonia water as an export product has poor quality, high content of naphthalene and its light oil, which can easily block production and transportation pipelines and storage tanks, making it difficult to export the product and having poor economic benefits. At the same time, the thiocyanate content in the ammonia distillation wastewater fluctuates, which has an impact on the ammonia distillation process. Summary of the invention

[0004] Aiming at the technical problems that the naphthalene content in ammonia water in the existing ammonia distillation process is relatively high, which easily causes pipeline blockage, and the cyanide and sulfide contents in the wastewater are relatively high, the present invention provides an ammonia distillation device and a method for improving the operation quality of the ammonia distillation process, adopts the technical idea of ​​sending acid gas from the bottom of the tower and sending side products to the outside, reduces the content of acidic corrosive factors such as sulfide and naphthalene in the ammonia distillation wastewater, and improves the quality of the sent concentrated ammonia water.

[0005] In a first aspect, the present invention provides an ammonia distillation device, comprising an ammonia distillation tower, an ammonia distillation tubular furnace, an ammonia fractionator, a condenser cooler, a reaction tower, a concentrated ammonia water tank, an adsorption tower, a residual ammonia water heat exchanger, and a vent tank; the residual ammonia water is divided into two parts, one part of the residual ammonia water is connected to the cold side medium inlet of the residual ammonia water heat exchanger through a pipeline, and the other part of the residual ammonia water is connected to the top of the ammonia distillation tower through a pipeline, and the cold side medium outlet of the residual ammonia water heat exchanger is connected to the 34th tower plate of the ammonia distillation tower through a pipeline; the feed inlet of the reaction tower is connected to the 14th tower plate of the ammonia distillation tower through a pipeline, and the discharge port of the reaction tower is connected to the ammonia distillation tower through a pipeline. The feed inlet of the ammonia fractionator is connected to the 27th plate of the ammonia distillation tower through a pipeline, the condensate outlet at the bottom of the ammonia fractionator is connected to the 25th plate of the ammonia distillation tower through a pipeline, the gas outlet at the top of the ammonia fractionator is connected to the feed inlet of the condenser cooler through a pipeline, the discharge port of the condenser cooler is connected to the feed inlet of the concentrated ammonia water tank through a pipeline, the discharge port of the ammonia water tank is connected to the feed inlet of the adsorption tower through a pipeline, and the discharge port of the adsorption tower is connected to the product delivery pipeline through a pipeline; the top of the ammonia distillation tower is connected to the pre-cooler through a pipeline, and the bottom of the ammonia distillation tower is connected to the feed inlet and discharge port of the ammonia distillation tube furnace through two pipelines respectively.

[0006] Furthermore, it also includes an asphalt tank and a vent tank. The discharge port at the bottom of the ammonia distillation tower is connected to the feed port of the asphalt tank through a pipeline, and the discharge port of the asphalt tank is connected to the vent tank through a pipeline.

[0007] Furthermore, the bottom of the ammonia evaporation tower is also connected to the heat medium inlet of the residual ammonia water heat exchanger through a pipeline, and the heat medium outlet of the residual ammonia water heat exchanger is connected to the biochemical unit through a pipeline.

[0008] Furthermore, there are multiple adsorption towers, which are connected in series or in parallel.

[0009] In a second aspect, the present invention provides a method for improving the operation quality of an ammonia distillation process, comprising the following steps: (1) The residual ammonia water in the blast condensation section is divided into two parts. One part enters the residual ammonia water heat exchanger and then enters the upper and middle part of the ammonia evaporation tower. The other part enters the top of the ammonia evaporation tower as the cold feed of the ammonia evaporation tower. (2) The remaining ammonia water entering the ammonia still tower enters from the 34th tray, and the liquid caustic soda enters from the 18th tray. The remaining ammonia water flows downward through the 14th tray and then flows from the ammonia still tower to the reaction tower. In the reaction tower, the remaining ammonia water and the liquid caustic soda are evenly mixed and then decompose the ammonium salt. The ammonium salt is then transported by the circulating pump at the bottom of the reaction tower to the 13th tray of the ammonia still tower, and then countercurrently contacts with the steam at the bottom of the tower for stripping; (3) The heat source of the ammonia distillation tower is provided by an ammonia distillation tubular furnace. The ammonia distillation wastewater is pumped out by the circulating pump at the bottom of the ammonia distillation tower, heated by the ammonia distillation tubular furnace, and then sent to the bottom of the ammonia distillation tower; (4) Another part of the remaining ammonia water enters from the top of the ammonia distillation tower. The top of the ammonia distillation tower is provided with a Larue ring packing layer at the 34th tower plate. When the bottom temperature of the ammonia distillation tower rises to 110°C, the top temperature of the ammonia distillation tower reaches 80°C, and the pressure is 0.03MPa, the top valve of the tower is opened to extract the acid gas from the top of the tower and send it to the primary cooler; (5) Ammonia gas produced from the side line of the ammonia still enters the bottom of the ammonia fractionator from the 27th tray. The temperature of ammonia gas produced from the top of the ammonia fractionator is controlled to be 103°C by adjusting the circulating cooling water. The condensate produced during the cooling process flows back into the ammonia still through the 25th tray. (6) In step (5), the ammonia gas is sent to a condenser cooler for condensation to obtain concentrated ammonia water, which is then discharged into a concentrated ammonia water storage tank for storage. The concentrated ammonia water is then sent to an adsorption tower for naphthalene removal and oil removal before being sent out.

[0010] Furthermore, in step (1), the ratio of the amount of residual ammonia water entering the residual ammonia water heat exchanger to the amount of residual ammonia water entering the top of the ammonia distillation tower is 3:1.

[0011] Furthermore, in step (3), part of the ammonia evaporation wastewater at the bottom of the ammonia evaporation tower is sent to the residual ammonia water heat exchanger to exchange heat with the incoming residual ammonia water, and after the heat exchange, the ammonia evaporation wastewater is sent to the coking wastewater treatment device for treatment.

[0012] Furthermore, in step (3), the bottom temperature of the ammonia evaporation tower is controlled to be 110°C and the bottom pressure is controlled to be 0.045 MPa; the asphalt produced at the bottom of the tower is discharged to the asphalt tank, and the slag is discharged by pumping and gravity. The asphalt produced at the bottom of the tower is regularly discharged to the asphalt tank to prevent the ammonia evaporation tower and the heat exchanger from being blocked; after the asphalt discharged to the asphalt tank is cooled, the separated water is sent to the tar ammonia water separation process for treatment, and the asphalt slag is sent to the coal preparation process.

[0013] Furthermore, in step (6), after the adsorption tower is saturated, it is back-flushed with steam at a flow rate of 1 t / h and a temperature of 200°C for 3 hours, and then the saturated adsorption tower packing is flushed and regenerated with ammonia wastewater at a flow rate of 2-4 t / h and a temperature of 100°C. The regeneration time is 5-10 hours.

[0014] The principle of the present invention is as follows: the present invention utilizes the difference in volatility between acidic gases such as H2S, CO2, HCN dissolved in residual ammonia water and NH3, and changes the main body of the ammonia evaporation tower from the original tower top to produce ammonia gas, and ammonia evaporation wastewater flows out from the tower bottom. The process of ammonia stripping and distillation in the tower is changed to the following gas-liquid mass transfer process: an acid gas distillation section between the top and the hot feed plate, an acid gas stripping section between the hot feed plate and the side line extraction plate, an ammonia stripping section between the side line outlet and the tower bottom, ammonia evaporation wastewater flows out from the tower bottom, acid gas is extracted from the tower top, ammonia is extracted from the side line, and the ammonia is condensed and introduced into the adsorption tower. After adsorption treatment in the adsorption tower, high-quality concentrated ammonia water is obtained.

[0015] The beneficial effects of the present invention are: (1) The present invention reduces the content of naphthalene in concentrated ammonia water and eliminates the pipeline blockage problem caused by naphthalene.

[0016] (2) The present invention uses tower top deacidification and adsorption tower adsorption to improve the quality of the concentrated ammonia solution delivered externally.

[0017] (3) The present invention removes S by deacidification 2- , HS - 、CO3 2- , HCO 3- The content of corrosive factors such as chlorine and chlorine can be reduced, the corrosion in the system can be reduced, the quality of the concentrated ammonia water sent out can be improved, and the sulfide content in the ammonia distillation wastewater can be reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, for ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0019] Figure 1 This is a schematic structural diagram of an ammonia distillation device according to a specific embodiment of the present invention; Figure 2 It is a comparison chart of the quality of concentrated ammonia water according to a specific embodiment of the present invention.

[0020] In the figure, 1-ammonia evaporation tower, 2-ammonia evaporation tubular furnace, 3-ammonia fractionator, 4-condenser cooler, 5-reaction tower, 6-concentrated ammonia water tank, 7-adsorption tower, 8-residual ammonia water heat exchanger, 9-vent tank. DETAILED DESCRIPTION

[0021] In order to enable those skilled in the art to better understand the technical solutions in the present invention, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work should fall within the scope of protection of the present invention.

[0022] Example 1 like Figure 1 As shown, an ammonia distillation device includes an ammonia distillation tower 1, an ammonia distillation tubular furnace 2, an ammonia fractionator 3, a condenser cooler 4, a reaction tower 5, a concentrated ammonia water tank 6, an adsorption tower 7, a residual ammonia water heat exchanger 8, and a vent tank 9; The remaining ammonia water is divided into two parts, one part of the remaining ammonia water is connected to the cold side medium inlet of the remaining ammonia water heat exchanger 8 through a pipeline, and the other part of the remaining ammonia water is connected to the top of the ammonia distillation tower 1 through a pipeline, and the cold side medium outlet of the remaining ammonia water heat exchanger 8 is connected to the 34th tower plate of the ammonia distillation tower 1 through a pipeline; the feed port of the reaction tower 5 is connected to the 14th tower plate of the ammonia distillation tower 1 through a pipeline, and the discharge port of the reaction tower 5 is connected to the 13th tower plate of the ammonia distillation tower 1 through a pipeline; the feed port of the ammonia decompressor 3 is connected to the 14th tower plate of the ammonia distillation tower 1 through a pipeline. The condensate outlet at the bottom of the ammonia decompressor 3 is connected to the 25th tray of the ammonia decompressor 1 through a pipeline, the gas outlet at the top of the ammonia decompressor 3 is connected to the feed port of the condenser cooler 4 through a pipeline, the discharge port of the condenser cooler 4 is connected to the feed port of the concentrated ammonia water tank 6 through a pipeline, the discharge port of the concentrated ammonia water tank 6 is connected to the feed port of the adsorption tower 7 through a pipeline, the discharge port of the adsorption tower 7 is connected to the product delivery pipeline through a pipeline, and the number of adsorption towers 7 is multiple, and they are connected in series or in parallel; The top of the ammonia distillation tower 1 is connected to the primary cooler through a pipeline, and the bottom of the ammonia distillation tower 1 is connected to the feed port and the discharge port of the ammonia distillation tube furnace 2 through two pipelines respectively. The discharge port at the bottom of the ammonia distillation tower 1 is connected to the feed port of the asphalt tank through a pipeline, and the discharge port of the asphalt tank is connected to the venting tank 9 through a pipeline; the bottom of the ammonia distillation tower 1 is also connected to the heat medium inlet of the residual ammonia water heat exchanger 8 through a pipeline, and the heat medium outlet of the residual ammonia water heat exchanger 8 is connected to the biochemical unit through a pipeline.

[0023] Example 2 108m 3 Taking the residual ammonia water treatment capacity of / h as an example, a method for improving the operation quality of the ammonia distillation process includes the following steps: (1) The residual ammonia water in the blast condensation section passes through the flotation oil remover, the residual ammonia water intermediate tank, the residual ammonia water tank, and the ceramic filter, a total of about 108m 3 / h, divided into two parts, one part is 81m 3 / h enters the residual ammonia water heat exchanger 8 and then enters the side of the ammonia distillation tower 1 for heat exchange. The other part 27m 3 / h remaining ammonia water enters the top of ammonia still 1 as cold feed of ammonia still 1; (2) The remaining ammonia water entering the ammonia still 1 enters from the 34th tray, and the liquid caustic soda with a concentration of 32% enters the ammonia still 1 through the 18th tray. The remaining ammonia water flows downward through the 14th tray and then flows from the ammonia still 1 to the reaction tower 5. In the reaction tower 5, the remaining ammonia water and the liquid caustic soda are mixed evenly and then decompose the ammonium salt. Then, it is transported by the circulating pump at the bottom of the reaction tower 5 and flows into the 13th tray of the ammonia still 1, and then contacts with the steam at the bottom of the tower in countercurrent for stripping. The volume of the reaction tower 5 is 70m 3 ; (3) The heat source of ammonia evaporation tower 1 is provided by ammonia evaporation tubular furnace 2. Ammonia evaporation wastewater is pumped out by the circulating pump at the bottom of ammonia evaporation tower 1, heated by ammonia evaporation tubular furnace 1, and then sent to the bottom of ammonia evaporation tower 1. The temperature at the bottom of ammonia evaporation tower 1 is controlled to be 110°C and the pressure at the bottom is 0.045MPa. Part of the ammonia evaporation wastewater at the bottom of ammonia evaporation tower 1 is sent to the residual ammonia water heat exchanger 8 to exchange heat with the residual ammonia water entering. After the heat exchange, the ammonia evaporation wastewater is sent to the coking wastewater treatment device for treatment. The asphalt produced at the bottom of the tower is discharged to the asphalt tank. After the asphalt discharged to the asphalt tank is cooled, it is sent to the tar ammonia water separation process for treatment. (4) Another part of the remaining ammonia water enters from the top of the ammonia still 1. The top of the ammonia still 1 is provided with a Larue ring packing layer at the 34th tower plate. When the bottom temperature of the ammonia still 1 rises to 110°C, the top temperature of the ammonia still 1 reaches 80°C, and the pressure is 0.03MPa, the top valve is opened to extract the top acid gas and send it to the front of the primary cooler; (5) Ammonia gas produced from the side line of ammonia still 1 enters the bottom of ammonia fractionator 3 from the 27th tray. The temperature of ammonia gas produced from the top of ammonia fractionator 3 is controlled to be 103°C by adjusting the circulating cooling water. The condensate produced during the cooling process flows back into ammonia still 1 through the 25th tray. (6) The side ammonia extraction flow rate is controlled by a regulating valve, and the ammonia in step (5) is sent to the condenser cooler 4 to be cooled to 40°C to obtain concentrated ammonia water, which is then discharged into the concentrated ammonia water storage tank 6 for storage. The concentrated ammonia water is then sent to the adsorption tower for naphthalene removal and de-oiling treatment, and then sent to the concentrated ammonia water system. After the adsorption tower is saturated, it is backwashed with steam at a flow rate of 1 t / h and a temperature of 200°C for 3 hours, and then the saturated adsorption tower packing is flushed and regenerated with ammonia wastewater at a flow rate of 2-4 t / h and a temperature of 100°C. The regeneration time is 5-10 hours. The regenerated wastewater is gravity-flowed into the nearby ammonia underground drain tank and sent to the tar ammonia water separation section.

[0024] Under the working conditions of this embodiment, the acid gas produced at the top of the ammonia distillation tower is 250m3 per hour. 3 / h, pH value of the wastewater at the bottom of the tower is 7~8, ammonia nitrogen ≤150mg / l, sulfide content ≤80mg / l, cyanide content ≤70mg / l, naphthalene removal rate of the adsorption tower is 90%, ammonia water mass concentration ≥20%, concentrated ammonia water output 3m 3 / h.

[0025] Figure 2 A comparison chart of the quality of the concentrated ammonia water delivered before and after the application of the present invention is shown, and it can be seen that the quality of the concentrated ammonia water is significantly improved.

[0026] Although the present invention has been described in detail by referring to the accompanying drawings and in combination with the preferred embodiments, the present invention is not limited thereto. Without departing from the spirit and essence of the present invention, a person skilled in the art may make various equivalent modifications or substitutions to the embodiments of the present invention, and these modifications or substitutions shall be within the scope of the present invention. Any person skilled in the art who is familiar with the present technical field can easily think of changes or substitutions within the technical scope disclosed by the present invention, and they shall be within the scope of protection of the present invention.

Claims

1. An ammonia distillation device, characterized in that: It includes an ammonia distillation tower, an ammonia distillation tubular furnace, an ammonia fractionator, a condenser cooler, a reaction tower, a concentrated ammonia water tank, an adsorption tower, a residual ammonia water heat exchanger, and a vent tank; the residual ammonia water is divided into two parts, one part of the residual ammonia water is connected to the cold side medium inlet of the residual ammonia water heat exchanger through a pipeline, and the other part of the residual ammonia water is connected to the top of the ammonia distillation tower through a pipeline, and the cold side medium outlet of the residual ammonia water heat exchanger is connected to the 34th tower plate of the ammonia distillation tower through a pipeline; the feed inlet of the reaction tower is connected to the 14th tower plate of the ammonia distillation tower through a pipeline, and the discharge port of the reaction tower is connected to the 13th tower plate of the ammonia distillation tower through a pipeline. The feed inlet of the ammonia fractionator is connected to the 27th plate of the ammonia distillation tower through a pipeline, the condensate outlet at the bottom of the ammonia fractionator is connected to the 25th plate of the ammonia distillation tower through a pipeline, the gas outlet at the top of the ammonia fractionator is connected to the feed inlet of the condenser cooler through a pipeline, the discharge port of the condenser cooler is connected to the feed inlet of the concentrated ammonia water tank through a pipeline, the discharge port of the ammonia water tank is connected to the feed inlet of the adsorption tower through a pipeline, and the discharge port of the adsorption tower is connected to the product delivery pipeline through a pipeline; the top of the ammonia distillation tower is connected to the pre-cooler through a pipeline, and the bottom of the ammonia distillation tower is connected to the feed inlet and discharge port of the ammonia distillation tube furnace through two pipelines respectively.

2. The ammonia distillation device according to claim 1, characterized in that: It also includes an asphalt tank and a vent tank. The discharge port at the bottom of the ammonia distillation tower is connected to the feed port of the asphalt tank through a pipeline, and the discharge port of the asphalt tank is connected to the vent tank through a pipeline.

3. The ammonia distillation device according to claim 2, characterized in that: The bottom of the ammonia distillation tower is also connected to the heat medium inlet of the residual ammonia water heat exchanger through a pipeline, and the heat medium outlet of the residual ammonia water heat exchanger is connected to the biochemical unit through a pipeline.

4. The ammonia distillation device according to claim 1, characterized in that: There are multiple adsorption towers, which are connected in series or in parallel.

5. A method for improving the operation quality of an ammonia distillation process by using the ammonia distillation device according to claim 1, characterized in that: The steps include: (1) The residual ammonia water in the blast condensation section is divided into two parts. One part enters the residual ammonia water heat exchanger and then enters the upper and middle part of the ammonia evaporation tower. The other part enters the top of the ammonia evaporation tower as the cold feed of the ammonia evaporation tower. (2) The remaining ammonia water entering the ammonia still tower enters from the 34th tray, and the liquid caustic soda enters from the 18th tray. The remaining ammonia water flows downward through the 14th tray and then flows from the ammonia still tower to the reaction tower. In the reaction tower, the remaining ammonia water and the liquid caustic soda are evenly mixed and then decompose the ammonium salt. The ammonium salt is then transported by the circulating pump at the bottom of the reaction tower to the 13th tray of the ammonia still tower, and then countercurrently contacts with the steam at the bottom of the tower for stripping; (3) The heat source of the ammonia distillation tower is provided by an ammonia distillation tubular furnace. The ammonia distillation wastewater is pumped out by the circulating pump at the bottom of the ammonia distillation tower, heated by the ammonia distillation tubular furnace, and then sent to the bottom of the ammonia distillation tower; (4) Another part of the remaining ammonia water enters from the top of the ammonia distillation tower. The top of the ammonia distillation tower is provided with a Larue ring packing layer at the 34th tower plate. When the bottom temperature of the ammonia distillation tower rises to 110°C, the top temperature of the ammonia distillation tower reaches 80°C, and the pressure is 0.03MPa, the top valve of the tower is opened to extract the acid gas from the top of the tower and send it to the primary cooler; (5) Ammonia gas produced from the side line of the ammonia still enters the bottom of the ammonia fractionator from the 27th tray. The temperature of ammonia gas produced from the top of the ammonia fractionator is controlled to be 103°C by adjusting the circulating cooling water. The condensate produced during the cooling process flows back into the ammonia still through the 25th tray. (6) In step (5), the ammonia gas is sent to a condenser cooler for condensation to obtain concentrated ammonia water, which is then discharged into a concentrated ammonia water storage tank for storage. The concentrated ammonia water is then sent to an adsorption tower for naphthalene removal and oil removal before being sent out.

6. The method for improving the operation quality of an ammonia distillation process in an ammonia distillation device according to claim 5, characterized in that: In step (1), the ratio of the residual ammonia water entering the residual ammonia water heat exchanger to the residual ammonia water entering the top of the ammonia distillation tower is 3:

1.

7. The method for improving the operation quality of an ammonia distillation process in an ammonia distillation device according to claim 5, characterized in that: In step (3), part of the ammonia evaporation wastewater at the bottom of the ammonia evaporation tower is sent to the residual ammonia water heat exchanger to exchange heat with the incoming residual ammonia water. After the heat exchange, the ammonia evaporation wastewater is sent to the coking wastewater treatment device for treatment.

8. The method for improving the operation quality of an ammonia distillation process in an ammonia distillation device according to claim 5, characterized in that: In step (3), the bottom temperature of the ammonia distillation tower is controlled to be 110°C and the bottom pressure is controlled to be 0.045 MPa; the asphalt produced at the bottom of the tower is discharged to the asphalt tank, and after the asphalt discharged to the asphalt tank is cooled, the separated water is sent to the tar ammonia water separation process for treatment, and the asphalt residue is sent to the coal preparation process.

9. The method for improving the operation quality of an ammonia distillation process in an ammonia distillation device according to claim 5, characterized in that: In step (6), after the adsorption tower is saturated, it is back-flushed with steam at a flow rate of 1 t / h and a temperature of 200°C for 3 hours, and then the saturated adsorption tower packing is flushed and regenerated with ammonia wastewater at a flow rate of 2-4 t / h and a temperature of 100°C. The regeneration time is 5-10 hours.

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