CN113998752A - Desulfurization wastewater concentration and flue gas heat and humidity recovery system and method - Google Patents
Desulfurization wastewater concentration and flue gas heat and humidity recovery system and method Download PDFInfo
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- CN113998752A CN113998752A CN202111660965.XA CN202111660965A CN113998752A CN 113998752 A CN113998752 A CN 113998752A CN 202111660965 A CN202111660965 A CN 202111660965A CN 113998752 A CN113998752 A CN 113998752A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
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Abstract
The invention discloses a desulfurization wastewater concentration and flue gas heat and humidity recovery system, which comprises a hydrophilic porous ceramic membrane component, a desulfurization tower, a hydrophilic component, an evaporator and a condenser, wherein the hydrophilic porous ceramic membrane component is provided with a first liquid inlet end and a first liquid outlet end; the hydrophilic component is provided with a second liquid inlet end and a second liquid outlet end, the second liquid outlet end is communicated with the liquid inlet end of the heat release side of the evaporator, and the liquid outlet end of the heat release side of the evaporator is communicated with the second liquid inlet end; and a third liquid outlet end is arranged on the desulfurizing tower, the third liquid outlet end is connected with a liquid inlet at the heat absorption side of the condenser, and a liquid outlet at the heat absorption side of the condenser is connected with the first liquid inlet end. The invention utilizes the waste heat of the flue gas to concentrate the desulfurized wastewater, thereby reducing the energy consumption of the system; the desulfurization wastewater is not directly contacted with the flue gas, so that the problem that the flue is corroded is solved.
Description
Technical Field
The invention relates to the technical field of flue gas heat and humidity recovery and desulfurization wastewater treatment, and particularly relates to a system and a method for concentrating desulfurization wastewater and recovering flue gas heat and humidity.
Background
Coal fired power plant can produce a large amount of desulfurization waste water in service, and desulfurization waste water contains a high salt content, pollutes greatly. With the strictness of environmental regulations around the world and the continuous enhancement of environmental awareness of people, the treatment and discharge requirements of desulfurization wastewater tend to zero discharge and no pollution. The mainstream desulfurization wastewater treatment technology at present has high cost, and a large amount of steam and electric energy are consumed for concentrating the desulfurization wastewater. The prior art discloses a device for concentrating wastewater by using the waste heat of clean flue gas of a coal-fired boiler, which comprises a dust remover, a desulfurizing tower, a chimney and a flue for the clean flue gas; the system also comprises a waste water tank, a waste water concentration component, a concentrated water tank, a pump station and a bypass waste water concentration flue, wherein the waste water concentration component is positioned in the bypass waste water concentration flue, and an induced draft fan is arranged in the left end of the bypass waste water concentration flue; the waste water concentration component comprises a waste water concentration cavity, a concentrated water collector and a demister, wherein the left end of the waste water concentration cavity is provided with an air inlet, and the right end of the waste water concentration cavity is provided with an air outlet; the inside atomizer that is equipped with of concentrated chamber left end of waste water, the outlet intercommunication of waste water pump station has the delivery pipe, and the concentrated chamber left end of waste water is equipped with heat exchanger. The comparison document adopts the technology of atomizing and evaporating the desulfurization wastewater, and has the problems that the droplets which are not completely evaporated corrode a flue and block a nozzle.
Disclosure of Invention
The invention provides a desulfurization waste water concentration and flue gas heat and humidity recovery system in order to solve the problems that the flue is corroded and the nozzle is blocked by incompletely evaporated liquid drops by adopting the technology of atomizing and evaporating desulfurization waste water in the prior art.
In order to solve the technical problems, the invention adopts the technical scheme that: a desulfurization waste water concentration and flue gas heat and humidity recovery system comprises a hydrophilic porous ceramic membrane component, a desulfurization tower, a hydrophilic component, an evaporator and a condenser, wherein the hydrophilic porous ceramic membrane component is used for performing heat and humidity exchange on desulfurization waste water flowing into the desulfurization tower and flue gas entering the desulfurization tower; the hydrophilic component is also provided with a second liquid inlet end and a second liquid outlet end, the second liquid outlet end is communicated with the liquid inlet end of the heat release side of the evaporator through a pipeline, and the liquid outlet end of the heat release side of the evaporator is communicated with the second liquid inlet end through a pipeline; a refrigerant pipeline of the evaporator and a refrigerant pipeline of the condenser form a closed channel; and a third liquid outlet end is arranged on the desulfurizing tower, the third liquid outlet end is communicated with a liquid inlet at the heat absorption side of the condenser through a pipeline, and a liquid outlet at the heat absorption side of the condenser is connected with the first liquid inlet end.
In the technical scheme, flue gas enters the hydrophilic porous ceramic membrane component through the first air inlet, the flue gas is humidified and cooled by intramembrane desulfurization wastewater of the hydrophilic porous ceramic membrane component, the flue gas humidified and cooled by the hydrophilic porous ceramic membrane component enters the desulfurization tower for desulfurization treatment, the desulfurization wastewater generated by the desulfurization tower exchanges heat with the heat absorption side of the condenser and then flows into the first liquid inlet of the hydrophilic porous ceramic membrane component, the hydrophilic porous ceramic membrane component performs membrane distillation on the desulfurization wastewater, the desulfurization wastewater is concentrated, and the concentrated desulfurization wastewater can be further treated by other components. And the flue gas flowing out of the desulfurizing tower and the hydrophilic component are discharged after being subjected to damp-heat recovery, and the water flow flowing out of the hydrophilic component and the heat release side of the evaporator are subjected to heat exchange and then flow back into the hydrophilic component. In the technical scheme, the temperature of the flue gas entering the desulfurizing tower is reduced, the humidity is increased, and the water evaporation in the wet desulfurizing process can be effectively reduced, so that the water consumption for desulfurizing is reduced; the desulfurization waste water is concentrated by using the waste heat of the flue gas, so that the energy consumption of the system is reduced; the desulfurization wastewater is not directly contacted with the flue gas, so that the problem that the flue is corroded is solved.
Preferably, the hydrophilic porous ceramic membrane module comprises a first box body and a plurality of hydrophilic ceramic membrane tubes penetrating through the first box body, wherein one end of each hydrophilic ceramic membrane tube forms the first liquid inlet end, and the other end of each hydrophilic ceramic membrane tube forms the first liquid outlet end; the first box body is also provided with the first air inlet end and the first air outlet end.
Preferably, the desulfurization waste water treatment device further comprises a triple box for treating desulfurization waste water, wherein the triple box is provided with a fourth liquid inlet end and a fourth liquid outlet end, the fourth liquid inlet end is communicated with the third liquid outlet end through a pipeline, and the fourth liquid outlet end is communicated with a liquid inlet at the heat absorption side of the condenser through a pipeline.
Preferably, the condenser further comprises a side branch pipeline, one end of the side branch pipeline is connected to a pipeline between the liquid inlet of the heat absorption side of the condenser and the fourth liquid outlet end, and the other end of the side branch pipeline is connected to a pipeline between the liquid outlet of the heat absorption side of the condenser and the first liquid inlet end.
Preferably, a first valve for adjusting the flow of the bypass pipeline is further arranged on the bypass pipeline.
Preferably, the desulfurization tower further comprises a water storage tank, the water storage tank is connected to a pipeline between the second liquid outlet end and the liquid inlet end of the heat release side of the evaporator, and the water storage tank is communicated with a third liquid inlet end arranged on the desulfurization tower through a pipeline.
Preferably, the hydrophilic component is a hydrophilic hollow fiber membrane component, the hydrophilic hollow fiber membrane component comprises a second box body and a plurality of hydrophilic hollow fiber membrane tubes penetrating the second box body, one end of each hydrophilic hollow fiber membrane tube forms the second liquid inlet end, and the other end of each hydrophilic hollow fiber membrane tube forms the second liquid outlet end; and a third air inlet end communicated with the second air outlet end and a third air outlet end communicated with an external chimney are formed on the second box body.
Preferably, an accident water pool is further connected to a pipeline between the first liquid inlet end and a liquid outlet on the heat absorption side of the condenser through a first branch pipe.
Preferably, a first cleaning pipeline is further communicated with a pipeline between the first branch pipe and the first liquid inlet end, an output pipeline for discharging concentrated desulfurization wastewater is connected to the first liquid outlet end, and a second cleaning pipeline for discharging cleaning water is connected to the output pipeline.
The invention provides a recovery method based on the cooperation of desulfurization wastewater concentration and flue gas heat and humidity recovery system, which comprises the following steps: flue gas generated by the boiler enters the hydrophilic porous ceramic membrane component from the first gas inlet end and performs heat and moisture exchange with desulfurization wastewater flowing in from the first liquid inlet end; the flue gas flowing out of the first gas outlet end of the hydrophilic porous ceramic membrane component enters a desulfurizing tower for desulfurization treatment, and the desulfurization wastewater generated by the desulfurizing tower enters a condenser for preheating, then flows back to the hydrophilic porous ceramic membrane component through the first liquid inlet end of the hydrophilic porous ceramic membrane component, and is concentrated; and the flue gas flowing out of the second gas outlet end of the desulfurizing tower enters the hydrophilic component for heat and moisture recovery and then is discharged, and the water flowing out of the second liquid outlet end of the hydrophilic component returns to the second liquid inlet end of the hydrophilic component after being cooled at the heat release side of the evaporator.
Compared with the prior art, the invention has the beneficial effects that: in the invention, the temperature of the flue gas entering the desulfurizing tower is reduced, the humidity is increased, and the moisture evaporation in the wet desulfurizing process can be effectively reduced, thereby reducing the water consumption for desulfurizing; the desulfurization waste water is concentrated by using the waste heat of the flue gas, so that the energy consumption of the system is reduced; the desulfurization wastewater is not directly contacted with the flue gas, so that the problem that the flue is corroded is solved. The system has the advantages that the heat pump formed by the evaporator and the condenser provides heat and cold simultaneously, the energy utilization rate is high, the temperature of the desulfurization wastewater is increased after the desulfurization wastewater is heated by the heat absorption side of the condenser, and the membrane distillation efficiency of the hydrophilic porous ceramic membrane component is higher. In addition, the water flowing out of the hydrophilic component can enter the hydrophilic component again for recycling after being cooled by the heat-releasing side of the evaporator, and an extra large amount of cooling water is not needed.
Drawings
FIG. 1 is a schematic structural diagram of a desulfurization wastewater concentration and flue gas heat and humidity recovery system in cooperation with the present invention;
FIG. 2 is a schematic structural diagram of a hydrophilic porous ceramic membrane module in the desulfurization wastewater concentration and flue gas heat and humidity recovery system of the invention;
FIG. 3 is a schematic structural diagram of a hydrophilic porous ceramic membrane module in the desulfurization wastewater concentration and flue gas heat and humidity recovery system provided with a first shell and a second shell;
FIG. 4 is a schematic structural diagram of hydrophilic components in the desulfurization wastewater concentration and flue gas heat and humidity recovery system of the present invention;
FIG. 5 is a schematic structural diagram of a hydrophilic component provided with a third shell and a fourth shell in the desulfurization wastewater concentration and flue gas heat and humidity recovery system.
In the drawings: 1. a hydrophilic porous ceramic membrane module; 2. a desulfurizing tower; 3. a hydrophilic component; 4. an evaporator; 5. a condenser; 6. a triple header; 7. a bypass conduit; 8. a water storage tank; 9. a first branch pipe; 10. an accident pool; 11. a first liquid inlet end; 12. a first liquid outlet end; 13. a first air inlet end; 14. a first air outlet end; 15. a first cleaning pipe; 16. an output pipe; 17. a second cleaning pipe; 21. a second air inlet end; 22. a second air outlet end; 23. a third liquid outlet end; 24. a third liquid inlet end; 31. a second liquid inlet end; 32. a second liquid outlet end; 33. a third air inlet end; 34. a third air outlet end; 101. a first case; 102. a hydrophilic ceramic membrane tube; 61. a fourth liquid inlet end; 62. a fourth liquid outlet end; 71. a first valve; 301. a second case; 302. a hydrophilic hollow fiber membrane tube; 18. a compressor; 19. an expansion valve; 51. a second valve; 81. a first water pump; 82. a third valve; 91. an accident valve; 92. an emergency water pump; 151. a third valve; 152. a third water pump; 161. a fifth valve; 162. a fifth water pump; 20. a main valve; 25. a chimney; 103. a first housing; 105. a second housing; 104. a first total liquid inlet end; 303. a third housing; 305. a fourth housing; 304. a second total inlet end.
Detailed Description
The drawings are for illustrative purposes only and are not to be construed as limiting the patent; for the purpose of better illustrating the embodiments, certain features of the drawings may be omitted, enlarged or reduced, and do not represent the size of an actual product; it will be understood by those skilled in the art that certain well-known structures in the drawings and descriptions thereof may be omitted. The positional relationships depicted in the drawings are for illustrative purposes only and are not to be construed as limiting the present patent.
The same or similar reference numerals in the drawings of the embodiments of the present invention correspond to the same or similar components; in the description of the present invention, it should be understood that if there are terms such as "upper", "lower", "left", "right", "long", "short", etc., indicating orientations or positional relationships based on the orientations or positional relationships shown in the drawings, it is only for convenience of description and simplicity of description, but does not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and therefore, the terms describing the positional relationships in the drawings are only used for illustrative purposes and are not to be construed as limitations of the present patent, and specific meanings of the terms may be understood by those skilled in the art according to specific situations.
The technical scheme of the invention is further described in detail by the following specific embodiments in combination with the attached drawings:
example 1
As shown in fig. 1 to 5, a desulfurization wastewater concentration and flue gas heat and humidity recovery system comprises a hydrophilic porous ceramic membrane module 1, a desulfurization tower 2, a hydrophilic component 3, an evaporator 4 and a condenser 5, wherein the hydrophilic porous ceramic membrane module 1 is used for performing heat and humidity exchange between desulfurization wastewater flowing into the desulfurization wastewater and flue gas entering the desulfurization tower, the hydrophilic porous ceramic membrane module 1 is provided with a first liquid inlet end 11 and a first liquid outlet end 12, the first liquid inlet end 11 and the first liquid outlet end 12 are respectively used for enabling desulfurization wastewater to flow in and out, the hydrophilic porous ceramic membrane module 1 is further provided with a first gas inlet end 13 and a first gas outlet end 14, the first gas outlet end 14 is communicated with a second gas inlet end 21 arranged on the desulfurization tower 2 through a pipeline, and a second gas outlet end 22 arranged on the desulfurization tower 2 is communicated with the hydrophilic component 3 through a pipeline; the hydrophilic component 3 is also provided with a second liquid inlet end 31 and a second liquid outlet end 32, the second liquid outlet end 32 is communicated with the liquid inlet end of the heat release side of the evaporator 4 through a pipeline, and the liquid outlet end of the heat release side of the evaporator 4 is communicated with the second liquid inlet end 31 through a pipeline; a refrigerant pipeline of the evaporator 4 and a refrigerant pipeline of the condenser 5 form a closed channel; the desulfurizing tower 2 is provided with a third liquid outlet end 23, the third liquid outlet end 23 is communicated with a liquid inlet at the heat absorption side of the condenser 5 through a pipeline, and a liquid outlet at the heat absorption side of the condenser 5 is connected with the first liquid inlet end 11. In this embodiment, the flue gas gets into hydrophilicity porous ceramic membrane subassembly 1 through first air inlet, the flue gas is by the intramembranous desulfurization waste water humidification cooling of hydrophilicity porous ceramic membrane subassembly 1, the flue gas through the humidification cooling of hydrophilicity porous ceramic membrane subassembly 1 gets into desulfurizing tower 2 and carries out desulfurization treatment, the desulfurization waste water that desulfurizing tower 2 produced flows into the first inlet of hydrophilicity porous ceramic membrane subassembly 1 after carrying out the heat exchange with condenser 5 heat absorption side, hydrophilicity porous ceramic membrane subassembly 1 carries out the membrane distillation to desulfurization waste water, desulfurization waste water is concentrated, the desulfurization waste water that is concentrated then can be done further processing with other subassemblies. The flue gas flowing out of the desulfurizing tower 2 and the hydrophilic component 3 are discharged after being subjected to damp heat recovery, and the water flow flowing out of the hydrophilic component 3 flows back into the hydrophilic component 3 after being subjected to heat exchange with the heat release side of the evaporator 4. The desulfurization waste water side of the hydrophilic porous ceramic membrane module 1 is maintained at a slight negative pressure to prevent the desulfurization waste water from leaking out of the membrane. In addition, it should be further noted that the refrigerant pipeline of the evaporator 4 and the refrigerant pipeline of the condenser 5 form a closed channel, a compressor 18 and an expansion valve 19 are arranged between the refrigerant pipeline of the evaporator 4 and the refrigerant pipeline of the condenser 5, a refrigerant outlet of the evaporator 4 is pressurized by the compressor 18 to become saturated vapor, and then enters the condenser 5 to be condensed into a liquid refrigerant, meanwhile, heat is released to heat the desulfurization wastewater, the refrigerant after heat release is depressurized by the expansion valve 19 to form a low-temperature saturated liquid, and then enters the evaporator 4 to be evaporated and absorbed to achieve refrigeration. Adopt the compression heat pump can heat desulfurization waste water and refrigeration cycle water simultaneously, but condenser 5 heatable desulfurization waste water specifically, and evaporimeter 4 can refrigeration cycle water, reduces the system energy consumption, makes the system more high-efficient, and the environmental protection benefit is showing. The temperature of the first liquid inlet end 11 and the first liquid outlet end 12 of the hydrophilic porous ceramic membrane component 1 is controlled to be 70 +/-5 ℃ and 80 +/-5 ℃ respectively; the temperature of the second liquid inlet end 31 and the second liquid outlet end 32 of the hydrophilic component 3 are respectively controlled at 70 +/-5 ℃ and 80 +/-5 ℃.
The hydrophilic porous ceramic membrane component 1 comprises a first box 101 and a plurality of hydrophilic ceramic membrane tubes 102 penetrating the first box 101, wherein a first liquid inlet end 11 is formed at one end of each hydrophilic ceramic membrane tube 102, and a first liquid outlet end 12 is formed at the other end of each hydrophilic ceramic membrane tube 102; the first box 101 further has a first inlet end 13 and a first outlet end 14 formed thereon. In this embodiment, desulfurization waste water flows into hydrophilic ceramic membrane tube 102 through first inlet end 11, and the flue gas gets into in first box 101 and sweeps across hydrophilic ceramic membrane tube 102 from first air inlet, then flows into desulfurizing tower 2 from first gas outlet, and hydrophilic ceramic membrane tube 102 need not to carry out hydrophobic modification, selects the tunica aperture at the micron level, only needs to keep little negative pressure with sulphur waste water side in the operation can avoid solution to permeate the membrane, and is with low costs and permeation flux obtains showing and improves. It should be noted that a main valve 20 is disposed on a pipeline connecting a liquid outlet of the heat absorption side of the condenser 5 and the first liquid inlet 11. The hydrophilic ceramic membrane tube 102 is in a nanometer scale, the contact angle of the hydrophilic ceramic membrane tube 102 is 40-80 degrees, the diameter of the hydrophilic ceramic membrane tube 102 is 6-15mm, and the length is 0.5-1.5 m. In addition, both ends of the hydrophilic ceramic membrane tube 102 penetrate through both opposite side surfaces of the first casing 101, and a first inlet end 11 formed at one end of the hydrophilic ceramic membrane tube 102 is used for inflow of desulfurization waste water that exchanges heat with the heat absorption side of the condenser 5, and a first outlet end 12 formed at the other end of the hydrophilic ceramic membrane tube 102 is used for outflow of concentrated desulfurization waste water. The first air inlet for allowing the flue gas to flow into the first box 101 and the first air outlet for allowing the flue gas to flow out of the first box 101 are oppositely arranged on the other two opposite side surfaces of the first box 101, so that the flue gas flowing into the first box 101 can be fully contacted with the peripheral wall of the hydrophilic ceramic membrane tube 102, and membrane distillation is performed on the desulfurization wastewater in the hydrophilic ceramic membrane tube 102. In addition, it should be noted that the first liquid inlet ends 11 of the plurality of hydrophilic ceramic membrane tubes 102 may be connected together, and then communicated with the liquid outlet on the heat absorption side of the condenser 5 through a pipeline; the first liquid outlet ends 12 of the plurality of hydrophilic ceramic membrane tubes 102 can be communicated together. Specifically, a first shell 103 wrapping the first liquid inlet end 11 may be further disposed on the first box 101, a first total liquid inlet end 104 is disposed on the first shell 103, the total liquid inlet end 104 is communicated with a liquid outlet on the heat absorption side of the condenser 5 through a pipeline, a second shell 105 wrapping the first liquid outlet end 12 may be further disposed on the first box 101, and a first total liquid outlet end is disposed on the second shell 105 and connected with an external pipeline.
In addition, the desulfurization waste water treatment device further comprises a triple box 6 for treating desulfurization waste water, the triple box 6 is provided with a fourth liquid inlet end 61 and a fourth liquid outlet end 62, the fourth liquid inlet end 61 is communicated with the third liquid outlet end 23 through a pipeline, and the fourth liquid outlet end 62 is communicated with a liquid inlet of the heat absorption side of the condenser 5 through a pipeline. In this embodiment, the desulfurization wastewater flowing out of the desulfurization tower 2 flows into the triple box 6 through the fourth liquid inlet end 61 through a pipeline, and after the desulfurization wastewater is treated by the triple box 6, the desulfurization wastewater flows out of the fourth liquid outlet end 62 to the liquid inlet on the heat absorption side of the condenser 5, and flows into the condenser 5 to exchange heat with the condenser 5, the preheated desulfurization wastewater flows into the hydrophilic porous ceramic membrane module 1 through the first liquid inlet end 11.
The condenser further comprises a side branch pipeline 7, one end of the side branch pipeline 7 is connected to a pipeline between the liquid inlet of the heat absorption side of the condenser 5 and the fourth liquid outlet end 62, and the other end of the side branch pipeline 7 is connected to a pipeline between the liquid outlet of the heat absorption side of the condenser 5 and the first liquid inlet end 11. In this embodiment, part of the desulfurization waste water flowing out of the triple box 6 may directly flow into the first liquid inlet end 11 through the bypass pipe 7 (without being preheated on the heat absorption side of the condenser 5) and be mixed with the desulfurization waste water preheated on the heat absorption side of the condenser 5. The temperature of the desulfurization waste water flowing into the first liquid inlet end 11 can be adjusted by arranging the bypass pipeline 7.
In addition, a first valve 71 for adjusting the flow rate of the bypass pipe 7 is provided in the bypass pipe 7. The bypass pipeline 7 is further provided with a first valve 71, and the flow rate of the bypass pipeline 7 can be adjusted through the arrangement of the first valve 71. In addition, a second valve 51 is also provided at the liquid inlet end of the heat absorption side of the condenser 5, and the flow rate flowing into the heat absorption side of the condenser 5 can be adjusted by the setting of the second valve 51.
Wherein, the water storage tank 8 is connected on the pipeline between the second liquid outlet end 32 and the liquid inlet end of the heat release side of the evaporator 4, and the water storage tank 8 is communicated with the third liquid inlet end 24 arranged on the desulfurizing tower 2 through the pipeline. In this embodiment, after the water in the hydrophilic component 3 exchanges heat with the flue gas flowing out from the desulfurization tower 2, the water flows out from the second liquid outlet end 32 of the hydrophilic component 3 to the water storage tank 8, and then flows back to the second liquid inlet end 31 of the hydrophilic component 3 after being cooled by the evaporator 4. It should be noted that the water storage tank 8 is communicated with a third liquid inlet end 24 arranged on the desulfurization tower 2 through a pipeline, so that the water in the water storage tank 8 can supplement water into the desulfurization tower 2. In addition, a first water pump 81 and a third valve 82 are provided in a pipe between the water storage tank 8 and the third liquid inlet 24.
In addition, the hydrophilic component 3 is a hydrophilic hollow fiber membrane module, which includes a second box 301 and a plurality of hydrophilic hollow fiber membrane tubes 302 penetrating the second box 301, a second liquid inlet end 31 formed at one end of the hydrophilic hollow fiber membrane tubes 302, and a second liquid outlet end 32 formed at the other end; the second box 301 further has a third air inlet end 33 communicated with the second air outlet end 22 and a third air outlet end 34 communicated with the external chimney 25. In this embodiment, the flue gas passing through the desulfurization tower 2 enters the second tank 301, the heat and moisture in the flue gas are absorbed by the cooling water in the hydrophilic hollow fiber membrane tube 302 and then discharged to the chimney 25, and the heated cooling water enters the evaporator 4 through the water storage tank 8 to be cooled, and then enters the hydrophilic hollow fiber membrane tube 302 again to recover heat and moisture from the flue gas. The water vapour in the flue gas condenses on the membrane surface and releases latent heat, which is transferred through the membrane to the cooling water side. Through this process, a large amount of heat and moisture in the flue gas can be recovered. The hydrophilic hollow fiber membrane tube 302 is adopted here because the flue gas temperature after desulfurization is low (about 50 ℃), high temperature resistance is not required, and the hollow fiber membrane tube is low in cost. In addition, it should be noted that the second liquid inlet ends 31 of the plurality of hydrophilic hollow fiber membrane tubes 302 may be connected together, and then communicated with the liquid outlet at the heat-releasing side of the evaporator through a pipeline; the second liquid outlet ends 32 of the plurality of hydrophilic hollow fiber membrane tubes 302 can be communicated together and then connected with a liquid inlet of the heat releasing side of the evaporator 4 through a pipeline. Specifically, a third shell 303 wrapping the second liquid inlet end 31 may be further disposed on the second box 301, a second total liquid inlet end 304 is disposed on the third shell 303, the second total liquid inlet end 304 is communicated with the liquid outlet of the heat release side of the evaporator 4 through a pipeline, a fourth shell 305 wrapping the second liquid outlet end 32 may be further disposed on the second box 301, and a second total liquid outlet end is disposed on the fourth shell 305 and is communicated with the liquid inlet of the heat release side of the evaporator 4.
An accident water tank 10 is connected to a pipeline between the first liquid inlet end 11 and a liquid outlet on the heat absorption side of the condenser 5 through a first branch pipe 9. When the desulfurization wastewater in the pipeline between the third liquid outlet end 23 and the first liquid inlet end 11 is in an accident, the desulfurization wastewater can be led out to the accident water tank 10 by opening the accident valve 91 and the accident water pump 92 which are arranged on the first branch pipe 9. It should be noted that the emergency valve 91, the emergency water pump 92 and the boiler control system adopt an interlocking protection mechanism, which specifically includes: when the boiler is stopped and tripped, the emergency valve 91 and the emergency water pump 92 are fully opened. The accident pool 10 can adopt an established accident pool 10 or be independently established, and the capacity of the accident pool 10 is not less than 8 hours of the generation amount of the desulfurization waste water.
Example 2
As shown in fig. 1, the difference from embodiment 1 is that a first cleaning pipeline 15 is further communicated with the pipeline between the first branch pipe 9 and the first liquid inlet end 11, an output pipeline 16 for discharging concentrated desulfurization wastewater is connected to the first liquid outlet end 12, and a second cleaning pipeline 17 for discharging cleaning water is connected to the output pipeline 16. In this embodiment, in order to clean the hydrophilic porous ceramic membrane module 1, a first cleaning pipeline 15 may be provided at the first inlet end 11, and cleaning water is injected into the first inlet end 11, enters the hydrophilic ceramic membrane tube 102, and is then discharged from the other end of the hydrophilic ceramic membrane tube 102 through the second cleaning pipeline 17. The first cleaning pipe 15 is provided with a third valve 151 and a third water pump 152, and the second cleaning pipe 17 is also provided with a fourth valve 171. The output pipe 16 is connected with a fifth valve 161 and a fifth water pump 162. The fifth water pump 162 is arranged at the first liquid outlet end 12 of the hydrophilic porous ceramic membrane module 1, so that the solution side of the hydrophilic ceramic membrane tube 102 can maintain micro negative pressure (-5 kPa to-0.5 kPa) during operation, thereby avoiding the solution from leaking out of the membrane tube.
Example 3
A recovery method based on desulfurization wastewater concentration and flue gas heat and humidity recovery system comprises the following steps: flue gas generated by the boiler enters the hydrophilic porous ceramic membrane module 1 from the first gas inlet end 13 and performs heat and moisture exchange with the desulfurization wastewater flowing in from the first liquid inlet end 11; the flue gas flowing out of the first gas outlet end 14 of the hydrophilic porous ceramic membrane module 1 enters a desulfurizing tower 2 for desulfurization treatment, and the desulfurization wastewater generated by the desulfurizing tower 2 enters a condenser 5 for preheating, then flows back to the hydrophilic porous ceramic membrane module 1 through the first liquid inlet end 11 of the hydrophilic porous ceramic membrane module 1, and is concentrated; the flue gas flowing out from the second gas outlet end 22 of the desulfurization tower 2 enters the hydrophilic module 3 for heat and moisture recovery and then is discharged, and the water flowing out from the second liquid outlet end 32 of the hydrophilic module 3 returns to the second liquid inlet end 31 of the hydrophilic module 3 after being cooled by the heat release side of the evaporator 4.
It should be understood that the above-described embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. Any modification, equivalent replacement, and improvement made within the spirit and principle of the present invention should be included in the protection scope of the claims of the present invention.
Claims (10)
1. The utility model provides a concentrated wet recovery system of flue gas heat in coordination of desulfurization waste water which characterized in that: the device comprises a hydrophilic porous ceramic membrane component (1) for performing heat and moisture exchange between desulfurization wastewater flowing into the hydrophilic porous ceramic membrane component and flue gas entering the hydrophilic porous ceramic membrane component, a desulfurization tower (2), a hydrophilic component (3), an evaporator (4) and a condenser (5), wherein the hydrophilic porous ceramic membrane component (1) is provided with a first liquid inlet end (11) and a first liquid outlet end (12) which are respectively used for inflow and outflow of the desulfurization wastewater, the hydrophilic porous ceramic membrane component (1) is also respectively provided with a first gas inlet end (13) and a first gas outlet end (14) which are used for inflow and outflow of the flue gas, the first gas outlet end (14) is communicated with a second gas inlet end (21) arranged on the desulfurization tower (2) through a pipeline, and a second gas outlet end (22) arranged on the desulfurization tower (2) is communicated with the hydrophilic component (3) through a pipeline; the hydrophilic component (3) is also provided with a second liquid inlet end (31) and a second liquid outlet end (32), the second liquid outlet end (32) is communicated with the liquid inlet end of the heat release side of the evaporator (4) through a pipeline, and the liquid outlet end of the heat release side of the evaporator (4) is communicated with the second liquid inlet end (32) through a pipeline; a refrigerant pipeline of the evaporator (4) and a refrigerant pipeline of the condenser (5) form a closed channel; and a third liquid outlet end (23) is arranged on the desulfurizing tower (2), the third liquid outlet end (23) is communicated with a liquid inlet of a heat absorption side of the condenser (5) through a pipeline, and a liquid outlet of the heat absorption side of the condenser (5) is connected with the first liquid inlet end (11).
2. The desulfurization wastewater concentration and flue gas heat and humidity recovery system as claimed in claim 1, wherein: the hydrophilic porous ceramic membrane component (1) comprises a first box body (101) and a plurality of hydrophilic ceramic membrane pipes (102) penetrating through the first box body (101), wherein one end of each hydrophilic ceramic membrane pipe (102) forms the first liquid inlet end (11), and the other end of each hydrophilic ceramic membrane pipe forms the first liquid outlet end (12); the first box body (101) is also provided with the first air inlet end (13) and the first air outlet end (14).
3. The desulfurization wastewater concentration and flue gas heat and humidity recovery system as claimed in claim 1, wherein: still including triple box (6) that is used for handling desulfurization waste water, triple box (6) are provided with fourth feed liquor end (61) and fourth play liquid end (62), fourth feed liquor end (61) with third play liquid end (23) is linked together through the pipeline, fourth play liquid end (62) with the inlet of the heat absorption side of condenser (5) is linked together through the pipeline.
4. The desulfurization wastewater concentration and flue gas heat and humidity recovery system as claimed in claim 3, wherein: still include other pipeline (7), the one end of other pipeline (7) is connected on the pipeline between the inlet of the heat absorption side of condenser (5) and fourth liquid outlet end, the other end of other pipeline (7) is connected on the pipeline between the liquid outlet of the heat absorption side of condenser (5) and first liquid inlet end (11).
5. The desulfurization wastewater concentration and flue gas heat and humidity recovery system as claimed in claim 4, wherein: and a first valve (71) for adjusting the flow of the bypass pipeline (7) is also arranged on the bypass pipeline (7).
6. The desulfurization wastewater concentration and flue gas heat and humidity recovery system as claimed in claim 1, wherein: still include storage water tank (8), storage water tank (8) are connected on the pipeline between the second goes out liquid end (32) and the inlet end of evaporimeter (4) exothermic side, storage water tank (8) are linked together through pipeline and third inlet end (24) of locating on desulfurizing tower (2).
7. The desulfurization wastewater concentration and flue gas heat and humidity recovery system as claimed in claim 1, wherein: the hydrophilic component (3) is a hydrophilic hollow fiber membrane component, the hydrophilic hollow fiber membrane component comprises a second box body (301) and a plurality of hydrophilic hollow fiber membrane tubes (302) penetrating the second box body (301), one end of each hydrophilic hollow fiber membrane tube (302) forms the second liquid inlet end (31), and the other end of each hydrophilic hollow fiber membrane tube forms the second liquid outlet end (32); and a third air inlet end (33) communicated with the second air outlet end (22) and a third air outlet end (34) communicated with an external chimney (25) are also formed on the second box body (301).
8. The desulfurization wastewater concentration and flue gas heat and humidity recovery system as claimed in claim 1, wherein: the first liquid inlet end (11) and a pipeline between liquid outlets on the heat absorption side of the condenser (5) are further connected with an accident water tank (10) through a first branch pipe (9).
9. The desulfurization wastewater concentration and flue gas heat and humidity recovery system as claimed in claim 8, wherein: the pipeline between the first branch pipe (9) and the first liquid inlet end (11) is also communicated with a first cleaning pipeline (15), the first liquid outlet end (12) is connected with an output pipeline (16) used for discharging concentrated desulfurization wastewater, and the output pipeline (16) is connected with a second cleaning pipeline (17) used for discharging cleaning water.
10. A recovery method based on the desulfurization wastewater concentration and flue gas heat and humidity recovery system of any one of claims 1 to 9, characterized by comprising the following steps: flue gas generated by the boiler enters the hydrophilic porous ceramic membrane component (1) from the first gas inlet end (13) and is subjected to heat and moisture exchange with desulfurization wastewater flowing in from the first liquid inlet end (11); flue gas flowing out of a first gas outlet end (14) of a hydrophilic porous ceramic membrane component (1) enters a desulfurizing tower (2) for desulfurization treatment, desulfurization wastewater generated by the desulfurizing tower (2) enters a condenser (5) for preheating, then flows back to the hydrophilic porous ceramic membrane component (1) through a first liquid inlet end (11) of the hydrophilic porous ceramic membrane component (1) for concentration; and the flue gas flowing out of the second gas outlet end (22) of the desulfurizing tower (2) enters the hydrophilic component (3) for heat and moisture recovery and then is discharged, and the water flowing out of the second liquid outlet end (32) of the hydrophilic component (3) flows through the heat releasing side of the evaporator (4) to be cooled and then returns to the second liquid inlet end (31) of the hydrophilic component (3).
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012236164A (en) * | 2011-05-12 | 2012-12-06 | Mitsubishi Heavy Ind Ltd | Aeration apparatus, seawater flue gas desulfurization apparatus including the same, and operation method of aeration apparatus |
| CN105944548A (en) * | 2016-07-05 | 2016-09-21 | 山东能工低碳科技有限公司 | Desulfurizing tower inlet flue duct and system with desulfurized wastewater concentration function |
| CN109812828A (en) * | 2019-02-19 | 2019-05-28 | 东莞理工学院 | A kind of moisture and waste heat recycling system based on the wet recyclable device of ceramic membrane heat |
| CN110508023A (en) * | 2019-08-27 | 2019-11-29 | 南京圣创科技有限公司 | A kind of method for utilizing flue gas heat crystallize outside tower in flue gas desulfurization |
-
2021
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012236164A (en) * | 2011-05-12 | 2012-12-06 | Mitsubishi Heavy Ind Ltd | Aeration apparatus, seawater flue gas desulfurization apparatus including the same, and operation method of aeration apparatus |
| CN105944548A (en) * | 2016-07-05 | 2016-09-21 | 山东能工低碳科技有限公司 | Desulfurizing tower inlet flue duct and system with desulfurized wastewater concentration function |
| CN109812828A (en) * | 2019-02-19 | 2019-05-28 | 东莞理工学院 | A kind of moisture and waste heat recycling system based on the wet recyclable device of ceramic membrane heat |
| CN110508023A (en) * | 2019-08-27 | 2019-11-29 | 南京圣创科技有限公司 | A kind of method for utilizing flue gas heat crystallize outside tower in flue gas desulfurization |
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