Ammonia desulfurization and decarbonization treatment system for industrial flue gas
Through the ammonia desulfurization and decarbonization treatment system, the reaction of ammonia water and sodium sulfate and ammonium bicarbonate is used to successfully remove carbon dioxide and sulfur dioxide from the flue gas, solving the problems of high cost and difficult treatment in the existing technology, and achieving efficient smoke Gas purification and resource recycling.
Patent Information
- Application Number
- CN202420158965.2
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-01-23
- Publication Date
- 2024-12-20
- Estimated Expiration
- 2034-01-23
AI Technical Summary
Existing carbon capture technologies such as the organic amine method have high operating costs, large waste emissions of the system and difficult to deal with, and lack cost-effective methods to convert CO2 into useful products.
The ammonia desulfurization and decarbonization treatment system is used to absorb carbon dioxide and sulfur dioxide in the flue gas through ammonia water, and the metathesis reaction of sodium sulfate and ammonium bicarbonate is obtained to obtain sodium bicarbonate, and sodium sulfate is precipitated through organic alcohol, and the organic is recovered by distillation method. Alcohol, achieves effective removal of carbon dioxide and sulfur dioxide in flue gas.
The net flue gas SO2 emissions have been zeroed, the smoke concentration is less than 5mg/Nm3, and sodium bicarbonate meets the requirements of GBT 1606-2008 Class III. The ammonium sulfate concentration is suitable, which reduces operating costs and improves system processing efficiency.
Smart Images
Figure CN222196480U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of industrial flue gas treatment, in particular to an ammonia-based desulfurization and decarbonization treatment system for industrial flue gas. Background Art
[0002] As the global climate change problem becomes increasingly serious, carbon emissions have become a common challenge faced by the world. Carbon capture, utilization and storage (CCUS) technology can convert CO2 into useful products or permanently store it, and is an important method of carbon emission reduction technology. Permanent storage of CO2 has high investment, no benefits, and is not attractive to enterprises. The conversion of CO2 into useful products is economically beneficial under certain conditions. It is very important to find a suitable technology. One of the main carbon capture technologies used worldwide is the organic amine method, but this method has problems such as high operating costs, large emissions of three wastes in the system, and difficulty in handling. Ammonia decarbonization is a mature method commonly used in the production of ammonium bicarbonate for small nitrogen fertilizers, and has certain economic benefits.
[0003] To this end, the utility model provides an ammonia desulfurization and decarbonization treatment system for industrial flue gas, which adopts ammonia water to absorb carbon dioxide and sulfur dioxide in the flue gas, adopts sulfuric acid to absorb ammonia in the flue gas, adopts sodium sulfate and ammonium bicarbonate to perform double decomposition reaction to obtain sodium bicarbonate, adopts organic alcohol precipitation to recover sodium sulfate, and adopts a distillation tower to recover organic alcohol. Utility Model Content
[0004] The utility model aims to provide an ammonia desulfurization and decarbonization treatment system for industrial flue gas, which adopts ammonia water to absorb carbon dioxide and sulfur dioxide in the flue gas, adopts sulfuric acid to absorb ammonia in the flue gas, adopts sodium sulfate and ammonium bicarbonate to react by double decomposition to obtain sodium bicarbonate, adopts organic alcohol to precipitate and recover sodium sulfate, and adopts a distillation tower to recover organic alcohol.
[0005] In order to achieve the above-mentioned purpose, the utility model proposes the following technical solution: an ammonia desulfurization and decarbonization treatment system for industrial flue gas, comprising:
[0006] A desulfurization, decarbonization and deammonification zone (1), wherein the desulfurization, decarbonization and deammonification zone (1) comprises a desulfurization, decarbonization and deammonification tower (11), wherein the desulfurization, decarbonization and deammonification tower (11) is provided with a first demister (113), a first liquid distributor (112), a first sieve plate (111), a gas-liquid splitting gas lift cap (19), a second demister (16), a second liquid distributor (15), a second sieve plate (14) and a cyclone oxidizer (13) in sequence from top to bottom;
[0007] The sodium bicarbonate separation zone (2) comprises a slurry tank (21), a slurry pump (22), a sodium bicarbonate thickener (23), a sodium bicarbonate centrifuge (24), a mother liquor heater (25), a cyclone gas-liquid separator (26) and an exhaust fan (27). The slurry tank (21) is connected to the sodium bicarbonate thickener (23) through the slurry pump (22), and the sodium bicarbonate thickener (23) is connected to the sodium bicarbonate centrifuge (24). The sodium bicarbonate centrifuge (24) is connected to the mother liquor heater (25), the mother liquor heater (25) is connected to the cyclone gas-liquid separator (26), the exhaust fan (27) is installed on the cyclone gas-liquid separator (26), the exhaust fan (27) extracts ammonia, carbon dioxide and water vapor from the top of the cyclone gas-liquid separator (26) back to the bottom area of the desulfurization, decarbonization and deammonification tower (11), and the liquid at the bottom of the cyclone gas-liquid separator (26) enters the mother liquor tank (31);
[0008] The sodium sulfate alcohol precipitation separation zone (3) comprises a mother liquor tank (31), a mother liquor pump (32), a sodium sulfate thickener (33), a sodium sulfate centrifuge (34), an ammonium sulfate alcohol solution tank (35), an ammonium sulfate alcohol solution pump (36), an ammonium sulfate alcohol liquid heat exchanger (37), a distillation tower (38), a condenser (39), an ammonium sulfate solution tank (310), and an ammonium sulfate solution pump (311). External organic alcohol and alcohol recovered from the distillation tower are added to the mother liquor tank (31), sodium sulfate is precipitated, and the sodium sulfate is precipitated through the mother liquor pump (32), the sodium sulfate thickener (33), The sodium sulfate centrifuge (34) is used for sodium sulfate recycling. The overflow liquid of the sodium sulfate thickener (33) and the mother liquor of the sodium sulfate centrifuge (34) flow into the ammonium sulfate alcohol solution tank (35) together, and then enter the ammonium sulfate alcohol liquid heat exchanger (37) for preheating through the ammonium sulfate alcohol solution pump (36), and then enter the distillation tower (38). The gaseous alcohol distilled from the distillation tower (38) is condensed through the condenser (39) and returned to the mother liquor tank (31). The solution in the ammonium sulfate alcohol liquid heat exchanger (37) enters the ammonium sulfate solution tank (310), and then is pumped to the outside through the ammonium sulfate solution pump (311) for concentration and crystallization.
[0009] Furthermore, in the utility model, the desulfurization, decarbonization and deammonification tower (11) is also provided with a cyclone oxidation pump (12), a desulfurization and decarbonization circulation pump (17), a desulfurization and decarbonization discharge pump (18) and a deammonification circulation pump (110), wherein the solution pumped out from the bottom of the tower by the desulfurization and decarbonization circulation pump (17) is distributed from the second liquid distributor (15) to a plurality of second sieve plates (14), the industrial flue gas contacts the solution on the second sieve plates (14), and the sulfur dioxide and carbon dioxide in the flue gas are dissolved in water and absorbed. The ammonia in the absorbed liquid is neutralized to form ammonium sulfite and ammonium bicarbonate. The desulfurization and decarbonization discharge pump (18) pumps the ammonium bicarbonate and ammonium sulfate solution at the bottom of the tower into the slurry tank (21). The sulfur dioxide in the flue gas dissolves in water and is neutralized by the ammonia in the absorbed liquid to form ammonium sulfite. The ammonium sulfite is then pumped into the cyclone oxidizer (13) by the cyclone oxidation pump (12) to mix with the oxidizing air supplied from the outside, and then jets into the lower diffusion section of the cyclone oxidizer (13), and then passes through the micropores at the lower part of the diffusion section to enter the slurry pool at the bottom of the tower.
[0010] Furthermore, in the utility model, the first sieve plate (111) and the second sieve plate (14) are one or more layers of sieve plates with variable apertures, and the sieve plate opening rate is adjusted as the flue gas load changes to keep the liquid holding layer height on the sieve plate stable.
[0011] Furthermore, in the utility model, an industrial flue gas inlet is provided on the desulfurization, decarbonization and deammonification tower (11), and the industrial flue gas inlet is located at the bottom of the second sieve plate (14).
[0012] Furthermore, in the utility model, the desulfurization, decarbonization and deammonification tower (11) is connected to a cooling water inlet pipe, and the cooling water inlet pipe is located at the bottom of the flue gas inlet.
[0013] Furthermore, in the present invention, the cyclone oxidizer (13) is connected to an oxygen inlet pipe, and the oxidizing air enters the cyclone oxidizer (13) through the oxygen inlet pipe to react with ammonium sulfite to generate ammonium sulfate.
[0014] Beneficial effects: The technical solution of this application has the following technical effects:
[0015] This system uses excess ammonia (or ammonia water) as a desulfurization and decarbonization agent to absorb sulfur dioxide and carbon dioxide in the flue gas to generate ammonium sulfite and ammonium bicarbonate. The ammonium sulfite is oxidized to generate ammonium sulfate. Sodium sulfate is used as an auxiliary agent to react with ammonium bicarbonate to generate sodium bicarbonate and ammonium sulfate. Sulfuric acid is used as a deamination agent to absorb ammonia in the tail gas to generate ammonium sulfate. Sodium bicarbonate separation uses a thickener and centrifugal separation slurry to obtain sodium bicarbonate solid and mother liquor. The mother liquor is heated to decompose the ammonium bicarbonate in the mother liquor. Sodium sulfate separation uses alcohol analysis, and the slurry is separated by a thickener and centrifugal separation to obtain sodium sulfate solid for recycling and mother liquor. Alcohol-water separation uses distillation to recover alcohol and reuse it. With this process, net flue gas SO2 emissions approach zero (0mg / Nm 3 ), smoke concentration is less than 5mg / Nm 3 , ammonium sulfate concentration is about 25%, and sodium bicarbonate meets the requirements of GBT 1606-2008 Class III.
[0016] It should be appreciated that all combinations of the foregoing concepts, as well as additional concepts described in greater detail below, may be considered part of the inventive subject matter of the present disclosure, provided such concepts are not mutually inconsistent.
[0017] The foregoing and other aspects, embodiments and features of the present invention can be more fully understood from the following description in conjunction with the accompanying drawings. Other additional aspects of the present invention, such as the features and / or beneficial effects of the exemplary embodiments, will be apparent from the following description or learned from the practice of the specific embodiments according to the teachings of the present invention. BRIEF DESCRIPTION OF THE DRAWINGS
[0018] The accompanying drawings are not intended to be drawn to scale. In the accompanying drawings, each identical or nearly identical component shown in various figures may be represented by the same reference numeral. For the sake of clarity, not every component is labeled in each figure. Now, embodiments of various aspects of the utility model will be described by way of example and with reference to the accompanying drawings, in which:
[0019] Figure 1 It is a schematic diagram of the utility model system.
[0020] In the figure, the meanings of the reference numerals are as follows: 1. desulfurization, decarbonization and deammonification zone; 2. sodium bicarbonate separation zone; 3. sodium sulfate alcohol precipitation separation zone; 11. desulfurization, decarbonization and deammonification tower; 12. cyclone oxidation pump; 13. cyclone oxidizer; 14. second sieve plate; 15. second liquid distributor; 16. second demister; 17. desulfurization and decarbonization circulation pump; 18. desulfurization and decarbonization discharge pump; 19. low resistance gas-liquid diversion lifting cap; 110. deammonification circulation pump; 111. first sieve plate; 112. second liquid distributor; 11 3. Second demister; 21. Slurry tank; 22. Slurry pump; 23. Sodium bicarbonate thickener; 24. Sodium bicarbonate centrifuge; 25. Mother liquor heater; 26. Cyclone gas-liquid separator; 27. Exhaust fan; 31. Mother liquor tank; 32. Mother liquor pump; 33. Sodium sulfate thickener; 34. Sodium sulfate centrifuge; 35. Ammonium thiol solution tank; 36. Ammonium thiol solution pump; 37. Ammonium thiol-liquid heat exchanger; 38. Distillation tower; 39. Condenser; 310. Ammonium thiol solution tank; 311. Ammonium thiol solution pump. DETAILED DESCRIPTION
[0021] In order to better understand the technical content of the utility model, specific embodiments are cited and described as follows in conjunction with the accompanying drawings. In this disclosure, various aspects of the utility model are described with reference to the accompanying drawings, and many illustrative embodiments are shown in the accompanying drawings. The embodiments of the present disclosure are not necessarily defined to include all aspects of the utility model. It should be understood that the various concepts and embodiments introduced above, as well as those described in more detail below, can be implemented in any of many ways, because the concepts and embodiments disclosed in the utility model are not limited to any implementation method. In addition, some aspects disclosed in the utility model can be used alone, or used in any appropriate combination with other aspects disclosed in the utility model.
[0022] like Figure 1 As shown, this embodiment provides a system for producing sodium bicarbonate and ammonium sulfate by ammonia-based flue gas desulfurization and decarbonization. The main equipment includes a desulfurization, decarbonization and deammoniation zone 1, a sodium bicarbonate separation zone 2 and a sodium sulfate alcohol precipitation separation zone 3.
[0023] Among them, the desulfurization, decarbonization and deammonification zone 1 includes: a desulfurization, decarbonization and deammonification tower 11, a cyclone oxidation pump 12, a cyclone oxidizer 13, a second sieve plate 14, a second liquid distributor 15, a second demister 16, a desulfurization and decarbonization circulation pump 17, a desulfurization and decarbonization discharge pump 18, a gas-liquid diversion gas lift cap 19, a deammonification circulation pump 110, a first sieve plate 111, a first liquid distributor 112 and a first demister 113.
[0024] Sodium bicarbonate separation zone 2: slurry tank 21, slurry pump 22, sodium bicarbonate thickener 23, sodium bicarbonate centrifuge 24, mother liquor heater 25, cyclone gas-liquid separator 26, exhaust fan 27.
[0025] Sodium sulfate alcohol precipitation separation zone 3: mother liquor tank 31, mother liquor pump 32, sodium sulfate thickener 33, sodium sulfate centrifuge 34, ammonium sulfate alcohol solution tank 35, ammonium sulfate alcohol solution pump 36, ammonium sulfate alcohol liquid heat exchanger 37, distillation tower 38, condenser 39, ammonium sulfate solution tank 310, ammonium sulfate solution pump 311.
[0026] In the name of this system, the flue gas flow process is as follows: industrial flue gas enters the desulfurization, decarbonization and deammonification tower 11 from the middle of the tower, the solution pumped out from the bottom of the tower by the desulfurization and decarbonization circulating pump 17 is distributed on the multi-layer second sieve plate 14 from the second liquid distributor 15, the industrial flue gas contacts with the solution on the second sieve plate 14, the sulfur dioxide and carbon dioxide in the flue gas are dissolved in water and neutralized by ammonia water in the absorption liquid to form ammonium sulfite and ammonium bicarbonate, the flue gas after desulfurization and decarbonization is defogged by the second demister 16, and then enters the deammonification area at the top of the tower through the low-resistance gas-liquid diversion lift cap 19, and contacts with the deammonification liquid pumped out by the deammonification circulating pump 110 on the multi-layer first sieve plate 111, wherein the deammonification liquid pumped out by the deammonification circulating pump 110 is provided by the first liquid distributor 112 and distributed on the multi-layer first sieve plate 113, the excess ammonia in the flue gas is absorbed by the sulfuric acid in the absorption liquid to form ammonium sulfate, and the deammonified flue gas is defogged by the second demister 113 and discharged from the top of the tower.
[0027] The ammonia flow process is as follows: external excess ammonia water is added to the inlet of the desulfurization and decarbonization circulation pump 17 and mixed with the solution from the tower, and then pumped to the second liquid distributor 15 in the tower through the desulfurization and decarbonization circulation pump 17, and then evenly distributed to the second sieve plate 14 through the liquid distributor 15. The solution contacts the flue gas, and the sulfur dioxide and carbon dioxide in the flue gas are dissolved in water and neutralized with ammonia to form ammonium sulfite and ammonium bicarbonate. Finally, the solution containing ammonium sulfite and ammonium bicarbonate falls into the solution pool at the bottom of the desulfurization tower. The excess ammonia in the flue gas is absorbed by sulfuric acid to form ammonium sulfate, which is also connected to the solution pool at the bottom of the tower.
[0028] The flow process of sodium bicarbonate is as follows: the desulfurization and decarbonization discharge pump 18 pumps the ammonium bicarbonate and ammonium sulfate solution at the bottom of the tower into the slurry tank 21, reacts with the sodium sulfate (and sodium sulfate recovered by the centrifuge) auxiliary agent input from the outside to generate a slurry containing sodium bicarbonate, ammonium sulfate and sodium sulfate. The slurry is pumped into the sodium bicarbonate thickener 23 through the slurry pump 22 for solid-liquid separation. The thick slurry at the bottom of the sodium bicarbonate thickener 23 enters the sodium bicarbonate centrifuge 24 for further solid-liquid separation, and the solid sodium bicarbonate is sent out for drying. The overflow liquid of the sodium bicarbonate thickener 23 and the mother liquor of the sodium bicarbonate thickener centrifuge 24 enter the mother liquor heater 25 together. After steam heating, the mother liquor enters the cyclone gas-liquid separator 26. The ammonium bicarbonate in the mother liquor decomposes into ammonia, carbon dioxide and water vapor. The exhaust fan 27 pumps ammonia, carbon dioxide and water vapor from the top back to the bottom area of the desulfurization, decarbonization and deammonification tower. The liquid at the bottom of the cyclone gas-liquid separator 26 enters the mother liquor tank 31.
[0029] The flow process of ammonium sulfate is as follows: sulfur dioxide in the flue gas is dissolved in water and neutralized by ammonia in the absorbent to generate ammonium sulfite, which is then pumped into the cyclone oxidizer 13 by the cyclone oxidation pump 12 to mix with the oxidizing air cyclone supplied from the outside, and then jets into the lower diffusion section of the cyclone oxidizer 13, and then passes through the micropores at the bottom of the diffusion section and enters the slurry pool at the bottom of the tower, where the ammonium sulfite is oxidized into ammonium sulfate. The ammonium sulfate solution after the removal of sodium bicarbonate, sodium sulfate, rectification and alcohol removal enters the ammonium sulfate solution tank 310, and then is pumped to the outside through the ammonium sulfate solution pump 311 for concentration and crystallization.
[0030] The flow process of organic alcohol is as follows: the external organic alcohol (or alcohol recovered from the distillation tower) liquid is added to the mother liquor tank 31, sodium sulfate is precipitated, and the sodium sulfate is recycled through the mother liquor pump 32, the sodium sulfate thickener 33, and the sodium sulfate centrifuge 34. The overflow liquid of the sodium sulfate thickener and the mother liquor of the sodium sulfate centrifuge flow to the ammonium sulfide alcohol solution tank 35. Then, it is preheated in the ammonium sulfide alcohol liquid heat exchanger 37 through the ammonium sulfide alcohol solution pump 36, and enters the distillation tower 38. The gaseous alcohol distilled from the distillation tower 38 is condensed by the condenser 39 and returned to the mother liquor tank. A steam heater is set at the bottom of the distillation tower.
[0031] The reaction equation is as follows:
[0032] Sulfur dioxide dissolves in water: SO2+H2O→H2SO3
[0033] Carbon dioxide dissolves in water: CO2+H2O→H2CO3
[0034] The reaction of sulfurous acid and ammonia: H2SO3+2NH3→(NH4)2SO3
[0035] Sulfurous acid reacts with oxygen: (NH4)2SO3+1 / 2O2→(NH4)2SO4
[0036] Carbonic acid reacts with ammonia: H2CO3+NH3→NH4HCO3
[0037] Ammonium bicarbonate reacts with sodium sulfate: 2NH4HCO3+N a2 SO4→2N a HCO3↓(supersaturated)+(NH4)2SO4
[0038] Dilute sulfuric acid reacts with ammonia: H2SO3+2NH3→(NH4)2SO3
[0039] This example was tested in a coal chemical self-provided thermal power plant, and the flue gas volume at the tower inlet was 1270119Nm 3 / h (standard state, wet basis, 6% O2), moisture content 7%, temperature 95°C, inlet SO2 concentration 6150mg / Nm 3 (Standard state, dry basis, 6% O2).
[0040] The designed desulfurization efficiency is not less than 99.7%, and the SO2 emission concentration is less than 5mg / Nm 3 (Standard state, dry basis, 6% O2), total smoke emission is less than 4mg / Nm 3 (Standard state, dry basis, 6% O2), sodium bicarbonate solid output 10t / h, meeting GBT 1606-2008 Class III requirements, ammonium sulfate solution output 90t / h (ammonium sulfate concentration 25%).
[0041] The main control indicators are as follows:
[0042]
[0043]
[0044] The main indicators are as follows:
[0045] name index ammonia 9750kg / h Sulfuric acid (98%) 50kg / h Sodium sulfate (anhydrous) 8500kg / h alcohol 100kg / h Low pressure steam 6.2t / h Cooling water 300t / h Process water 38.7t / h Power consumption 430kWh Smoke resistance 3500Pa Reducing carbon dioxide emissions 5.23t / h Sulfur dioxide emission concentration <h2 style=";text-align:left;direction:ltr"><5mg / Nm3<h2 style=";text-align:left;direction:ltr"> Dust emission concentration <h2 style=";text-align:left;direction:ltr"><5mg / Nm3<h2 style=";text-align:left;direction:ltr">
[0046] The standard parts used in this application document can all be purchased from the market and can be customized according to the description in the specification and drawings. The specific connection methods of each part adopt conventional means such as mature bolts, rivets, welding, etc. in the prior art. The machinery, parts and equipment all adopt conventional models in the prior art. The control method is automatic control through a controller. The control circuit of the controller can be implemented through simple programming by technicians in this field, which is common knowledge in the field. This application is mainly used to protect mechanical devices, so this application no longer explains the control method and circuit connection in detail.
[0047] Although the present invention has been disclosed as above with preferred embodiments, it is not intended to limit the present invention. A person with ordinary knowledge in the technical field to which the present invention belongs may make various changes and modifications without departing from the spirit and scope of the present invention. Therefore, the protection scope of the present invention shall be determined by the definition of the claims.
Claims
1. An ammonia-based desulfurization and decarbonization treatment system for industrial flue gas, characterized by: include: A desulfurization, decarbonization and deammonification zone (1), wherein the desulfurization, decarbonization and deammonification zone (1) comprises a desulfurization, decarbonization and deammonification tower (11), wherein the desulfurization, decarbonization and deammonification tower (11) is provided with a first demister (113), a first liquid distributor (112), a first sieve plate (111), a gas-liquid splitting gas lift cap (19), a second demister (16), a second liquid distributor (15), a second sieve plate (14) and a cyclone oxidizer (13) in sequence from top to bottom; The sodium bicarbonate separation zone (2) comprises a slurry tank (21), a slurry pump (22), a sodium bicarbonate thickener (23), a sodium bicarbonate centrifuge (24), a mother liquor heater (25), a cyclone gas-liquid separator (26) and an exhaust fan (27). The slurry tank (21) is connected to the sodium bicarbonate thickener (23) through the slurry pump (22), and the sodium bicarbonate thickener (23) is connected to the sodium bicarbonate centrifuge (24). The sodium bicarbonate centrifuge (24) is connected to the mother liquor heater (25), the mother liquor heater (25) is connected to the cyclone gas-liquid separator (26), the exhaust fan (27) is installed on the cyclone gas-liquid separator (26), the exhaust fan (27) extracts ammonia, carbon dioxide and water vapor from the top of the cyclone gas-liquid separator (26) back to the bottom area of the desulfurization, decarbonization and deammonification tower (11), and the liquid at the bottom of the cyclone gas-liquid separator (26) enters the mother liquor tank (31); The sodium sulfate alcohol precipitation separation zone (3) comprises a mother liquor tank (31), a mother liquor pump (32), a sodium sulfate thickener (33), a sodium sulfate centrifuge (34), an ammonium sulfate alcohol solution tank (35), an ammonium sulfate alcohol solution pump (36), an ammonium sulfate alcohol liquid heat exchanger (37), a distillation tower (38), a condenser (39), an ammonium sulfate solution tank (310), and an ammonium sulfate solution pump (311). The mother liquor tank (31) is used to place external organic alcohol and alcohol recovered by the distillation tower (38). The sodium sulfate is centrifuged and reused after passing through the mother liquor pump (32), the sodium sulfate thickener (33), and the sodium sulfate centrifuge (34). The ammonium alcohol solution tank (35) is used to collect the overflow liquid of the sodium sulfate thickener (33) and the mother liquor of the sodium sulfate centrifuge (34); the ammonium sulfate alcohol solution pump (36) is used to pump the ammonium sulfate alcohol solution in the ammonium sulfate alcohol solution tank (35) into the ammonium sulfate alcohol liquid heat exchanger (37) for preheating; the distillation tower (38) is used to rectify the gaseous alcohol; the condenser (39) is used to condense the distilled gaseous alcohol and return it to the mother liquor tank (31); the ammonium sulfate solution tank (310) is used to collect the solution in the ammonium sulfate alcohol liquid heat exchanger (37); and the ammonium sulfate solution pump (311) is used to pump the solution in the ammonium sulfate solution tank (310) to the outside for concentration and crystallization.
2. The ammonia desulfurization and decarbonization treatment system for industrial flue gas according to claim 1 is characterized in that: The desulfurization, decarbonization and deammonification tower (11) is also provided with a cyclone oxidation pump (12), a desulfurization and decarbonization circulation pump (17), a desulfurization and decarbonization discharge pump (18) and a deammonification circulation pump (110), wherein the desulfurization and decarbonization circulation pump (17) is used to distribute the solution pumped out from the bottom of the tower onto a plurality of second sieve plates (14) through a second liquid distributor (15), and the industrial flue gas contacts the solution on the second sieve plates (14), and sulfur dioxide and carbon dioxide in the flue gas are dissolved in water and absorbed by the liquid. Ammonia water is neutralized to generate ammonium sulfite and ammonium bicarbonate. The desulfurization and decarbonization discharge pump (18) is used to pump the ammonium bicarbonate and ammonium sulfate solution at the bottom of the tower into the slurry tank (21). The cyclone oxidation pump (12) is used to pump the ammonium sulfite into the cyclone oxidizer (13). The cyclone oxidizer (13) is used to cyclone-mix the pumped ammonium sulfite with the oxidation air supplied from the outside, and jet it into the lower diffusion section of the cyclone oxidizer (13), and enter the slurry pool at the bottom of the tower through the micropores at the lower part of the diffusion section.
3. The ammonia desulfurization and decarbonization treatment system for industrial flue gas according to claim 1 is characterized in that: The first sieve plate (111) and the second sieve plate (14) are one or more layers of sieve plates with variable apertures, and the aperture ratio of the sieve plates is adjusted as the flue gas load changes, so as to keep the height of the liquid holding layer on the sieve plates stable.
4. The ammonia desulfurization and decarbonization treatment system for industrial flue gas according to claim 1 is characterized by: The desulfurization, decarbonization and deammonification tower (11) is provided with an industrial flue gas inlet, and the industrial flue gas inlet is located at the bottom of the second sieve plate (14).
5. The ammonia desulfurization and decarbonization treatment system for industrial flue gas according to claim 1 is characterized in that: The desulfurization, decarbonization and deammonification tower (11) is connected to a cooling water inlet pipe, and the cooling water inlet pipe is located at the bottom of the flue gas inlet.
6. The ammonia desulfurization and decarbonization treatment system for industrial flue gas according to claim 1 is characterized by: The cyclone oxidizer (13) is connected to an oxygen inlet pipe, and the oxidizing air enters the cyclone oxidizer (13) through the oxygen inlet pipe to react with ammonium sulfite to generate ammonium sulfate.