Comprehensive waste gas treatment device for synthetic ammonia system

Abstract

The utility model relates to a comprehensive waste gas treatment device for a synthetic ammonia system. Comprising a shift stripping tail gas unit, a sulfur-containing tail gas pipeline of a low-temperature methanol washing device, a low-pressure oxygen pipeline of an air separation device and a fuel gas storage tank, a sulfur-containing tail gas pipeline of the low-temperature methanol washing device, a low-pressure oxygen pipeline of the air separation device and the fuel gas storage tank are respectively connected with an inlet of the combustion furnace, and an outlet of the combustion furnace is connected with the first gas-liquid separator through the sulfur recovery unit; a gas phase outlet of the first gas-liquid separator, the conversion steam stripping tail gas unit, the fuel gas storage tank and the air pipeline are respectively connected with an inlet of the incinerator, an outlet of the incinerator is connected with the boiler through the heat exchange unit, and a flue gas outlet of the boiler is connected with the chimney through the denitration device and the desulfurization device; the waste gas in the ammonia synthesis system can be uniformly treated according to properties, desulfurization and denitration devices are not independently arranged, and linkage design of tail gas treatment of the whole system is realized, so that the advantages of investment saving and environment friendliness are achieved.

Description

Technical Field

[0001] The utility model relates to the technical field of synthetic ammonia systems, and particularly relates to a comprehensive waste gas treatment device for a synthetic ammonia system. Background Art

[0002] Multiple exhaust gases are generated in the synthetic ammonia system, such as the exhaust gas produced in the conversion stripping tower, the exhaust gas produced in the low-temperature methanol washing device, etc.; according to the industry's conventional settings, multiple corresponding exhaust gas treatment devices are designed according to the components, characteristics, and flow rates of different exhaust gases; that is, multiple sets of combustion torches, desulfurization equipment, etc. will be set in a set of synthetic ammonia systems, which not only occupy a large area, require a large equipment investment, but also are not convenient to operate; further, taking the stripping exhaust gas produced by the conversion device as an example, it is usually treated by sending it to the torch for combustion or sending it to the sulfur recovery for combustion; taking the torch combustion as an example, the torch combustion method not only wastes resources, but also has the risk of polluting the environment; taking the sulfur recovery combustion as an example, since this exhaust gas contains ammonia, the combustion stability of ammonia is higher than that of hydrogen sulfide. To process this exhaust gas with a relatively small flow rate, the design specifications of the combustion furnace for sulfur recovery need to be improved, resulting in a large increase in the investment in sulfur recovery; in addition, when the sulfur recovery adopts the sulfur production process, due to under-oxygen combustion, the combustion is incomplete. The components of the exhaust gas after combustion are hydrogen 1.25, nitrogen 10.9, carbon monoxide 3.1, carbon dioxide 45.3, hydrogen sulfide 0.28, sulfur dioxide 0.14, and water 39.03 (mole fraction). Since this exhaust gas contains carbon monoxide and hydrogen, and their content exceeds 10% of their lower explosion limit, if it is directly sent to the boiler for combustion, it will lead to an increase in the explosion area division of the boiler area, resulting in an increase in the investment in the boiler device and requiring separate treatment. Summary of the Utility Model

[0003] The purpose of the utility model is to provide a comprehensive waste gas treatment device for a synthetic ammonia system to overcome the defects in the prior art.

[0004] To achieve the above purpose, the utility model provides the following technical solutions:

[0005] A comprehensive waste gas treatment device for a synthetic ammonia system includes a conversion stripping exhaust gas unit, a sulfur-containing exhaust gas pipeline of a low-temperature methanol washing device, a low-pressure oxygen pipeline of an air separation device, and a fuel gas storage tank; the sulfur-containing exhaust gas pipeline of the low-temperature methanol washing device, the low-pressure oxygen pipeline of the air separation device, and the fuel gas storage tank are respectively connected to the inlet of a combustion furnace, and the outlet of the combustion furnace is connected to a first gas-liquid separator through a sulfur recovery unit; the gas-phase outlet of the first gas-liquid separator, the conversion stripping exhaust gas unit, the fuel gas storage tank, and an air pipeline are respectively connected to the inlet of an incinerator, the outlet of the incinerator is connected to a boiler through a heat exchange unit, and the flue gas outlet of the boiler is connected to a chimney through a denitration device and a desulfurization device.

[0006] The beneficial effects of the present utility model are as follows: By arranging a combustion furnace to burn the sulfur-containing tail gas from the low-temperature methanol washing device and the low-pressure oxygen in the air separation device, the purpose of sulfur recovery in the subsequent process is achieved. Furthermore, the gas phase from sulfur recovery, fuel gas, shift stripping tail gas, etc. enter the incinerator for incineration. After incineration, the heat is recovered, and the tail gas is treated by the denitration device and desulfurization device equipped in the boiler, so as to reduce the difficulty of waste gas treatment in the synthetic ammonia system, and while recovering sulfur from the tail gas, a set of desulfurization and denitration devices are used to treat the waste gas of the entire synthetic ammonia system.

[0007] Preferably, the sulfur recovery unit includes a first steam generator. The outlet of the combustion furnace is connected to the first heat exchange channel of the first steam generator. The liquid phase outlet of the first heat exchange channel is connected to a liquid sulfur pool. The gas phase outlet of the first heat exchange channel is connected to a number of serially arranged sulfur recovery components. The gas phase outlet of the last sulfur recovery component is connected to a first gas-liquid separator. The liquid phase outlet of the first gas-liquid separator is connected to the liquid sulfur pool.

[0008] Preferably, the sulfur recovery component includes a steam heater and a sulfur reactor. The inlet of the first heat exchange channel of the steam heater is connected to the outlet of the first heat exchange channel of the first steam generator or the outlet of the first heat exchange channel of the previous sulfur reactor. The outlet of the first heat exchange channel of the steam heater is connected to the inlet of the corresponding sulfur reactor. The material outlet of the sulfur reactor is connected to the liquid sulfur pool through a corresponding sulfur condenser. The gas phase outlet of the sulfur reactor is connected to the inlet of the first heat exchange channel of the next steam heater or the inlet of the first gas-liquid separator.

[0009] Preferably, the inlet of the second heat exchange channel of the first steam generator is connected to a low-pressure boiler feed water pipeline. The outlet of the second heat exchange channel of the first steam generator is connected to a 0.5 MPa steam pipe network.

[0010] Preferably, the inlet of the second channel of the steam heater is connected to a 4 MPa steam pipe network. The outlet of the second channel of the steam heater is connected to a condensate recovery storage tank.

[0011] Preferably, the heat exchange unit includes a steam superheater. The outlet of the incinerator is connected to the first pipeline of the second steam generator through the first pipeline of the steam superheater. The first pipeline of the second steam generator is connected to the inlet of the boiler through the first channel of the fresh air heat exchanger. The air pipeline is connected to the inlet of the incinerator through a blower and the second channel of the fresh air heat exchanger.

[0012] Preferably, the inlet of the second pipeline of the second steam generator is connected to a low-pressure boiler feed water pipeline. The outlet of the second pipeline of the second steam generator is connected to the inlet of the second pipeline of the steam superheater. The outlet of the second pipeline of the steam superheater is connected to a 0.6 MPa superheated steam pipe network.

[0013] Preferably, the shift stripping tail gas unit includes a shift ammonia scrubbing tower. The liquid phase outlet of the shift ammonia scrubbing tower is connected to the shift stripping tower through the first channel of the first condenser. The gas phase outlet of the shift stripping tower is connected to the second channel of the first condenser and the first channel of the second condenser, and then to the second gas-liquid separator. The gas phase outlet of the second gas-liquid separator is connected to the incinerator.

[0014] Preferably, the liquid phase outlet of the second gas-liquid separator is connected to the coal gasification and coal grinding device. The inlet of the second channel of the second condenser is connected to the circulating cooling water supply pipeline, and the outlet of the second channel of the second condenser is connected to the circulating cooling water return pipeline.

[0015] An integrated waste gas treatment device for a synthetic ammonia system made according to the above scheme. In essence, the present invention uniformly treats the waste gas in the synthetic ammonia system according to relevant properties, avoiding the separate design of tail gas treatment devices for each process, which leads to an increase in equipment investment. Moreover, due to the large number of tail gas treatment devices, the non-compliance discharge rate increases, posing a potential environmental hazard to the enterprise. By sending the sulfur-containing tail gas from the low-temperature methanol washing device, the low-pressure oxygen, and the fuel gas from the air separation device into the combustion furnace for combustion, the present invention can not only recover and utilize heat, reduce the requirements for combustion equipment, but also facilitate the effective recovery of sulfur. Further, the tail gas after sulfur recovery, together with the fuel gas, the shift stripping tail gas, etc., enters the incinerator for combustion, and the denitrification and desulfurization systems of the boiler device are used to treat the nitrogen oxides and sulfides in the tail gas, eliminating the need for separately installed desulfurization and denitrification devices with high investment, realizing the linkage design of the whole system's tail gas treatment, thus achieving the advantages of saving investment, effectively utilizing heat energy, and being environmentally friendly. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 is a schematic structural diagram of the present invention.

[0017] In the figure: 1, sulfur-containing tail gas pipeline; 2, low-pressure oxygen pipeline; 3, fuel gas storage tank; 4, combustion furnace; 5, first gas-liquid separator; 6, air pipeline; 7, incinerator; 8, boiler; 9, denitrification device; 10, desulfurization device; 11, chimney; 12, first steam generator; 13, liquid sulfur tank; 14, steam heater; 15, sulfur reactor; 16, sulfur condenser; 17, low-pressure boiler feed water pipeline; 18, 0.5 MPa steam pipe network; 19, 4 MPa steam pipe network; 20, condensate recovery storage tank; 21, steam superheater; 22, second steam generator; 23, fresh air heat exchanger; 24, blower; 25, 0.6 MPa superheated steam pipe network; 26, shift ammonia scrubbing tower; 27, first condenser; 28, shift stripping tower; 29, second condenser; 30, second gas-liquid separator; 31, coal gasification and coal grinding device; 32, circulating cooling water supply pipeline; 33, circulating cooling water return pipeline. Detailed implementation manners

[0018] Next, the technical solutions in the embodiments of the present utility model will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present utility model.

[0019] Refer to Figure 1 As shown, the present utility model is a comprehensive waste gas treatment device for a synthetic ammonia system, including a shift stripping tail gas unit, a sulfur-containing tail gas pipeline 1 of a low-temperature methanol washing device, a low-pressure oxygen pipeline 2 of an air separation device, and a fuel gas storage tank 3; the sulfur-containing tail gas pipeline 1 of the low-temperature methanol washing device, the low-pressure oxygen pipeline 2 of the air separation device, and the fuel gas storage tank 3 are respectively connected to the inlet of a combustion furnace 4, and the outlet of the combustion furnace 4 is connected to a first gas-liquid separator 5 through a sulfur recovery unit; the gas-phase outlet of the first gas-liquid separator 5, the shift stripping tail gas unit, the fuel gas storage tank 3, and an air pipeline 6 are respectively connected to the inlet of an incinerator 7, the outlet of the incinerator 7 is connected to a boiler 8 through a heat exchange unit, and the flue gas outlet of the boiler 8 is connected to a chimney 11 through a denitration device 9 and a desulfurization device 10. The present utility model can perform hierarchical treatment on waste gas according to the properties of waste gas in the synthetic ammonia system, effectively recover the heat of waste gas combustion and the sulfur contained in the waste gas, and perform unified treatment through the denitration device 9 and the desulfurization device 10 in the boiler system on the premise of unified treatment of waste gas, and achieve the characteristics of environmental friendliness through up-to-standard discharge. The above settings can achieve the purpose of reducing the investment and construction cost and facilitating operation.

[0020] Furthermore, the sulfur recovery unit includes a first steam generator 12, the outlet of the combustion furnace 4 is connected to the first heat exchange channel of the first steam generator 12, the liquid-phase outlet of the first heat exchange channel is connected to a liquid sulfur pool 13, the gas-phase outlet of the first heat exchange channel is connected to a plurality of serially arranged sulfur recovery components, the gas-phase outlet of the last sulfur recovery component is connected to the first gas-liquid separator 5, and the liquid-phase outlet of the first gas-liquid separator 5 is connected to the liquid sulfur pool 13. In the present utility model, the first steam generator 12 is provided to realize the recovery and utilization of the heat in the tail gas, and a plurality of serially arranged sulfur recovery components are provided to realize the recovery of sulfur elements in the tail gas. Further, the first gas-liquid separator 5 is provided to realize the further recovery of sulfur elements, which can not only improve the emergency benefit, but also reduce the subsequent tail gas treatment load (this treatment load refers to the treatment load of the incinerator 7 and the treatment load of the desulfurization device 10).

[0021] Further, the sulfur recovery unit includes a steam heater 14 and a sulfur reactor 15. The inlet of the first heat exchange channel of the steam heater 14 is connected to the outlet of the first heat exchange channel of the first steam generator 12 or the outlet of the first heat exchange channel of the previous sulfur reactor 15. The outlet of the first heat exchange channel of the steam heater 14 is connected to the inlet of the corresponding sulfur reactor 15. The material outlet of the sulfur reactor 15 is connected to the liquid sulfur tank 13 through the corresponding sulfur condenser 16. The gas phase outlet of the sulfur reactor 15 is connected to the inlet of the first heat exchange channel of the next steam heater 14 or the inlet of the first gas-liquid separator 5. It should be clear that there are multiple sulfur recovery units in the present utility model (which can be set to two sets, three sets, four sets, etc. of sulfur recovery units according to actual situations). Its series design can achieve cascaded recovery of sulfur at different temperatures, so as to improve the sulfur recovery efficiency, reduce the subsequent load, and achieve the purpose of stable operation of the system.

[0022] Further, the inlet of the second heat exchange channel of the first steam generator 12 is connected to the low-pressure boiler feed water pipe 17, and the outlet of the second heat exchange channel of the first steam generator 12 is connected to the 0.5 MPa steam network 18. In the present utility model, the waste gas from the combustion furnace 4 is used to exchange heat with the demineralized water in the first steam generator 12, and the heat energy of the waste gas is utilized to achieve the purpose of by-product 0.5 MPa steam.

[0023] Further, the inlet of the second channel of the steam heater 14 is connected to the 4 MPa steam network 19, and the outlet of the second channel of the steam heater 14 is connected to the condensate recovery storage tank 20. In the present utility model, the heat source in the steam heater 14 is used to heat the waste gas, so as to achieve the characteristic of sulfur recovery.

[0024] Further, the heat exchange unit includes a steam superheater 21. The outlet of the incinerator 7 is connected to the first pipe of the second steam generator 22 through the first pipe of the steam superheater 21. The first pipe of the second steam generator 22 is connected to the inlet of the boiler 8 through the first channel of the fresh air heat exchanger 23. The air pipe 6 is connected to the inlet of the incinerator 7 through the blower 24 and the second channel of the fresh air heat exchanger 23. The heat exchange unit in the present utility model mainly includes two parts. One part is the heat exchange part for heating demineralized water to produce 0.6 MPa superheated steam, and the other part is the air preheating part for preheating air to meet the requirements of the incinerator 7. In the present utility model, the waste gas heat in the incinerator 7 is fully utilized in the heat exchange unit and then enters the boiler 8, and is subsequently treated by the corresponding denitration device and desulfurization device.

[0025] Further, the second pipeline inlet of the second steam generator 22 is connected to the low-pressure boiler feed water pipeline 17, the second pipeline outlet of the second steam generator 22 is connected to the second pipeline inlet of the steam superheater 21, and the second pipeline outlet of the steam superheater 21 is connected to the 0.6 MPa superheated steam pipe network 25.

[0026] Further, the shift stripping tail gas unit includes a shift ammonia scrubbing tower 26. The liquid phase outlet of the shift ammonia scrubbing tower 26 is connected to the shift stripping tower 28 through the first channel of the first condenser 27. The gas phase outlet of the shift stripping tower 28, the second channel of the first condenser 27, and the first channel of the second condenser 29 are connected to the second gas-liquid separator 30. The gas phase outlet of the second gas-liquid separator 30 is connected to the incinerator 7.

[0027] Further, the liquid phase outlet of the second gas-liquid separator 30 is connected to the coal gasification and pulverizing device 31; the second channel inlet of the second condenser 29 is connected to the circulating cooling water supply pipeline 32, and the second channel outlet of the second condenser 29 is connected to the circulating cooling water return pipeline 33.

[0028] A treatment process using a comprehensive treatment device for waste gas in a synthetic ammonia system, the process comprising the following steps:

[0029] Step 1: The sulfur-containing tail gas in the sulfur-containing tail gas pipeline 1 of the low-temperature methanol washing device, the oxygen in the low-pressure oxygen pipeline 2 of the air separation device, and the fuel gas in the fuel gas storage tank 3 enter the combustion furnace 4 for combustion. The flow rate of oxygen entering the combustion furnace 4 is controlled by the corresponding valve on the low-pressure oxygen pipeline 2, so as to control the molar ratio of hydrogen sulfide to sulfur dioxide in the tail gas after combustion in the combustion furnace 4 to be lower than 2:1, so as to complete the conversion of all hydrogen sulfide gas, and the excess sulfur dioxide is removed by the subsequent desulfurization device 10;

[0030] Step 2: The components of the tail gas after combustion in the combustion furnace 4 are: hydrogen 1.35, nitrogen 11.7, carbon monoxide 3.3, carbon dioxide 47.12, hydrogen sulfide 6.92, carbonyl sulfide 1.69, sulfur dioxide 4.33, and water 23.59. The tail gas after combustion enters the first heat exchange channel of the first steam generator 12 to exchange heat with the demineralized water from the low-pressure boiler feed water pipeline 17. The steam in the second heat exchange channel of the first steam generator 12 after heat exchange enters the 0.5 MPa steam pipe network 18, and the tail gas after heat exchange enters the first heat exchange channel of the steam heater 14 for heating; the temperature of the tail gas after heat exchange is 170-180 °C, and the tail gas heated by the steam heater 14 is 240-250 °C;

[0031] Step 3: The tail gas heated by the steam heater 14 enters the corresponding sulfur reactor 15 for reaction. The liquid phase after the reaction enters the corresponding sulfur condenser 16 for condensation, and after condensation, it is sent into the liquid sulfur pool 13 for recovery. The tail gas after the reaction in the sulfur reactor 15 enters the first heat exchange pass of the next steam heater 14 for heating. The composition of the tail gas entering the first heat exchange pass of the next steam heater 14 is: hydrogen 1.39, nitrogen 12.12, carbon monoxide 3.46, carbon dioxide 50.55, hydrogen sulfide 2.53, carbonyl sulfide 0.02, sulfur dioxide 1.27, water 28.66;

[0032] Step 4: The tail gas enters the first heat exchange pass of the next steam heater 14 for heating. After the tail gas is heated to 205 - 215 °C, it is sent into the corresponding sulfur reactor 15 for reaction. The liquid phase after the reaction enters the corresponding sulfur condenser 16 for condensation, and after condensation, it is sent into the liquid sulfur pool 13 for recovery. The tail gas after the reaction in the sulfur reactor 15 enters the first heat exchange pass of the subsequent steam heater 14 for heating. The composition of the tail gas entering the first heat exchange pass of the subsequent steam heater 14 is: hydrogen 1.43, nitrogen 12.38, carbon monoxide 3.54, carbon dioxide 51.67, hydrogen sulfide 0.58, carbonyl sulfide 0.02, sulfur dioxide 0.29, water 30.09;

[0033] Step 5: The tail gas enters the first heat exchange pass of the subsequent steam heater 14 for heating. After the tail gas is heated to 200 - 210 °C, it is sent into the corresponding sulfur reactor 15 for reaction. The liquid phase after the reaction enters the corresponding sulfur condenser 16 for condensation, and after condensation, it is sent into the liquid sulfur pool 13 for recovery. The tail gas after the reaction in the sulfur reactor 15 enters the first gas-liquid separator 5 for gas-liquid separation. The liquid phase separated by gas-liquid separation enters the liquid sulfur pool 13 for recovery, and the gas phase separated by gas-liquid separation enters the incinerator 7. The composition of the tail gas entering the first gas-liquid separator 5 is: hydrogen 1.43, nitrogen 12.46, carbon monoxide 3.56, carbon dioxide 51.99, hydrogen sulfide 0.24, carbonyl sulfide 0.01, sulfur dioxide 0.12, water 30.19;

[0034] Step 6: The ammonia-containing waste liquid in the shift ammonia scrubbing tower 26 enters the shift stripping tower 28 through the first channel of the first condenser 27. The shift stripping tower 28 strips out the ammonia and non-condensable gas in the waste liquid. The gas phase sequentially passes through the gas phase outlet of the shift stripping tower 28, the second channel of the first condenser 27, and the first channel of the second condenser 29 and enters the second gas-liquid separator 30 for gas-liquid separation. The liquid phase after gas-liquid separation enters the coal gasification and pulverization device 31, and the gas phase after gas-liquid separation enters the incinerator 7;

[0035] Step 7: The air in the air pipeline 6 enters the incinerator 7 through the blower 24 and the second channel of the fresh air heat exchanger 23;

[0036] Step 8: The fuel gas in the fuel gas storage tank 3, the gas phase of the first gas-liquid separator 5 in Step 5, the gas phase of the second gas-liquid separator 30 in Step 6, and the air passing through the second channel of the fresh air heat exchanger 23 in Step 7 jointly enter the incinerator 7 for combustion. The gas components after being incinerated in the incinerator 7 are: carbon dioxide 34.3, nitrogen 41.9, water 17.7, sulfur dioxide 1.1, oxygen 5, nitrogen oxides at 200 mg / Nm3, and no longer contain combustible gas;

[0037] Step 9: The gas after being incinerated in the incinerator 7 exchanges heat through the first pipeline of the steam superheater 21, the first pipeline of the second steam generator 22, and the first channel of the fresh air heat exchanger 23; the gas after heat exchange enters the boiler 8, and then the nitrogen oxides in the tail gas are removed by the denitration device 9, and the sulfur dioxide in the tail gas is removed by the desulfurization device 10. Finally, the qualified tail gas is discharged through the chimney 11;

[0038] The demineralized water in the low-pressure boiler feed water pipeline 17 enters the second pipeline of the second steam generator 22 for heat exchange and then enters the second pipeline of the steam superheater 21 for further heat exchange. The generated steam enters the 0.6 MPa superheated steam pipe network 25.

[0039] The present utility model is a transformation of the existing synthetic ammonia system. By the properties and characteristics of the different waste gases produced in the synthetic ammonia system, part of the tail gas is first used for combustion to recover the heat and sulfur in the tail gas, and then the tail gas after recovering sulfur is mixed with other tail gases and enters the incinerator for combustion to further utilize the heat. Finally, combustion is carried out through the boiler and combined with the denitration device 9 and the desulfurization device 10 to achieve up-to-standard discharge; the present utility model can uniformly treat the waste gases in the synthetic ammonia system, and use the denitration and desulfurization systems of the boiler device to treat the nitrogen oxides and sulfides in the tail gas, without separately setting up desulfurization and denitration devices with relatively high investment, realizing the linkage design of the whole-system tail gas treatment, so as to achieve the characteristics of saving investment, effectively utilizing heat energy, and environmental friendliness.

[0040] Although the embodiments of the present utility model have been shown and described, for those of ordinary skill in the art, it can be understood that various changes, modifications, substitutions, and variations can be made to these embodiments without departing from the principles and spirit of the present utility model. The scope of the present utility model is defined by the appended claims and their equivalents.

Claims

1. An integrated treatment device for waste gas in an ammonia synthesis system, characterized in that, It includes a conversion stripping tail gas unit, a sulfur-containing tail gas pipeline (1) of a low-temperature methanol washing device, a low-pressure oxygen pipeline (2) of an air separation device, and a fuel gas storage tank (3); The sulfur-containing tail gas pipeline (1) of the low-temperature methanol washing device, the low-pressure oxygen pipeline (2) of the air separation device, and the fuel gas storage tank (3) are respectively connected to the inlet of a combustion furnace (4), and the outlet of the combustion furnace (4) is connected to a first gas-liquid separator (5) through a sulfur recovery unit; The gas-phase outlet of the first gas-liquid separator (5), the conversion stripping tail gas unit, the fuel gas storage tank (3), and an air pipeline (6) are respectively connected to the inlet of an incinerator (7), the outlet of the incinerator (7) is connected to a boiler (8) through a heat exchange unit, and the flue gas outlet of the boiler (8) is connected to a chimney (11) through a denitration device (9) and a desulfurization device (10).

2. The integrated treatment device for waste gas of an ammonia synthesis system according to claim 1, characterized in that, The sulfur recovery unit includes a first steam generator (12), the outlet of the combustion furnace (4) is connected to the first heat exchange channel of the first steam generator (12), the liquid-phase outlet of the first heat exchange channel is connected to a liquid sulfur pool (13), the gas-phase outlet of the first heat exchange channel is connected to a plurality of serially arranged sulfur recovery components, the gas-phase outlet of the last sulfur recovery component is connected to the first gas-liquid separator (5), and the liquid-phase outlet of the first gas-liquid separator (5) is connected to the liquid sulfur pool (13).

3. The comprehensive treatment device for waste gas of an ammonia synthesis system according to claim 2, characterized in that, The sulfur recovery component includes a steam heater (14) and a sulfur reactor (15), The inlet of the first heat exchange channel of the steam heater (14) is connected to the outlet of the first heat exchange channel of the first steam generator (12) or the outlet of the first heat exchange channel of the previous sulfur reactor (15), the outlet of the first heat exchange channel of the steam heater (14) is connected to the inlet of the corresponding sulfur reactor (15), the material outlet of the sulfur reactor (15) is connected to the liquid sulfur pool (13) through a corresponding sulfur condenser (16), and the gas-phase outlet of the sulfur reactor (15) is connected to the inlet of the first heat exchange channel of the next steam heater (14) or the inlet of the first gas-liquid separator (5).

4. The comprehensive treatment device for waste gas of an ammonia synthesis system according to claim 2 or 3, characterized in that, The inlet of the second heat exchange channel of the first steam generator (12) is connected to a low-pressure boiler feed water pipeline (17), and the outlet of the second heat exchange channel of the first steam generator (12) is connected to a 0.5 MPa steam pipe network (18).

5. The comprehensive treatment device for waste gas of an ammonia synthesis system according to claim 3, characterized in that, The inlet of the second channel of the steam heater (14) in the sulfur recovery component is connected to a 4 MPa steam pipe network (19), and the outlet of the second channel of the steam heater (14) is connected to a condensate recovery storage tank (20).

6. The comprehensive treatment device for waste gas of an ammonia synthesis system according to claim 1, wherein, The heat exchange unit includes a steam superheater (21), the outlet of the incinerator (7) is connected to the first pipeline of a second steam generator (22) through the first pipeline of the steam superheater (21), and the first pipeline of the second steam generator (22) is connected to the inlet of the boiler (8) through the first channel of a fresh air heat exchanger (23); The air pipeline (6) is connected to the inlet of the incinerator (7) through a blower (24) and the second channel of the fresh air heat exchanger (23).

7. An integrated waste gas treatment device for an ammonia synthesis system according to claim 6, characterized in that, The second pipeline inlet of the second steam generator (22) is connected to the low-pressure boiler feed water pipeline (17), the second pipeline outlet of the second steam generator (22) is connected to the second pipeline inlet of the steam superheater (21), and the second pipeline outlet of the steam superheater (21) is connected to the 0.6 MPa superheated steam pipe network (25).

8. The integrated treatment device for waste gas of an ammonia synthesis system according to claim 1, wherein, The shift stripping tail gas unit includes a shift ammonia scrubbing tower (26). The liquid phase outlet of the shift ammonia scrubbing tower (26) is connected to the shift stripping tower (28) through the first channel of the first condenser (27). The gas phase outlet of the shift stripping tower (28) is connected to the second channel of the first condenser (27) and the first channel of the second condenser (29) and then to the second gas-liquid separator (30). The gas phase outlet of the second gas-liquid separator (30) is connected to the incinerator (7).

9. The integrated treatment device for waste gas of an ammonia synthesis system according to claim 8, characterized in that, The liquid phase outlet of the second gas-liquid separator (30) is connected to the coal gasification and pulverizing device (31); the second channel inlet of the second condenser (29) is connected to the circulating cooling water supply pipeline (32), and the second channel outlet of the second condenser (29) is connected to the circulating cooling water return pipeline (33).

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