CN113860613B - High-salt wastewater thermal vibration cyclone salt extraction system - Google Patents
High-salt wastewater thermal vibration cyclone salt extraction system Download PDFInfo
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
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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
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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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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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
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
Abstract
The invention relates to a high-salt wastewater thermal vibration cyclone salt extraction system. The system adopts softening resin to separate monovalent salt from divalent salt and high-valence salt, the monovalent salt is circulated in the system only and does not carry out extraction treatment, the overflow amount of the monovalent salt in the system is balanced with the added monovalent salt amount of wastewater, the divalent salt and the high-valence salt are extracted by adopting a thermal vibration cyclone evaporator, the system is divided into two paths after softening pretreatment equipment, one path comprises a 5-time concentration NF component and a 2-time concentration SWRO reverse osmosis unit, the other path comprises a 3-time concentration SWRO reverse osmosis unit and a thermal vibration cyclone evaporator, the softening pretreatment equipment separates the monovalent salt from the divalent salt and the high-valence salt, the monovalent salt enters the 5-time concentration NF component and is used as circulating regeneration liquid of the softening resin after subsequent treatment, the monovalent salt replaces the divalent salt and the high-valence salt attached to the softening resin, the replaced divalent salt and the high-valence salt are subjected to salt extraction treatment by the thermal vibration cyclone evaporator, the divalent salt and the high-valence salt solid is extracted, and zero wastewater discharge is realized.
Description
Technical Field
The invention relates to the technical field of salt extraction of wastewater, in particular to a high-salt wastewater thermal vibration cyclone salt extraction system.
Background
With the technical improvement of new and old kinetic energy conversion in chemical plants, the coking wastewater is not used for blast furnace slag flushing, and is not used for sintering machine water, converter flue gas cooling and other processes, so that the coke dry quenching rate is improved, the coke quality requirement of the blast furnace is met, the coke wet quenching water consumption is very low, and the coking wastewater cannot be digested by downstream.
At present, national environmental protection laws and regulations require that each enterprise is required to realize zero discharge of wastewater, and more coking enterprises in China are transformed or are being transformed, so that the zero discharge of coking wastewater is a development trend. The advanced treatment of the biochemical effluent by utilizing the wastewater can reach the direct discharge standard, eliminate the defects of the wastewater treatment process at the present stage, relieve the environmental protection pressure and avoid the environmental protection risk.
The high-salt wastewater contains a large amount of suspended matters (gypsum particles, siO) 2 Hydroxides of aluminum and iron), active silicon, COD, chloride, fluoride, calcium, magnesium, aluminum, iron and trace heavy metal ions such as arsenic, cadmium, chromium, mercury, etc., are directly discharged to cause serious environmental hazard. In order to thoroughly solve the problem of coking wastewater, the coking wastewater needs to be subjected to advanced treatment and recycling, and biochemical effluent is subjected to double-membrane and salt extraction advanced treatment, so that zero emission of the coking wastewater is realized.
The existing typical desalination technology is that mixed salt in high-salt wastewater is extracted by evaporation concentration, and is indirectly heated by steam, so that the energy consumption is high, and more than 1t of steam is required to be consumed for evaporating 1t of desulfurization liquid. In addition, the monovalent salt, the divalent salt and the sodium thiocyanate in the concentrated salt are mixed together and cannot be sold out, and are often treated as hazardous solid waste.
If the concentrated mixed salt is separated by adopting the subsequent process, a solvent crystallization process is mostly adopted, and sodium thiocyanate in the concentrated mixed salt solution is dissolved and separated by adopting volatile first solvents such as methanol, ethanol and the like, and then single salt is prepared by evaporation crystallization. The method needs to consume a large amount of organic solvent for separating the mixed salt, and 0.5t of solvent is needed for crystallizing the 1t sodium thiocyanate product. Meanwhile, the safety operation requirement and the construction cost of the class A solvent on the production device are relatively high. And the solvent needs to be recovered, and a large amount of heat energy is required for multiple evaporation and crystallization.
In addition, the above-mentioned salt extraction method cannot extract pure water from high-salt wastewater, and cannot realize recycling of resources.
In view of this, a new high-salt wastewater thermal vibration cyclone salt extraction system is needed to solve the problems that the high-salt wastewater in the prior art cannot extract pure water and the extracted mixed salt has no economic value.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a high-salt wastewater thermal vibration rotational flow salt extraction system which can extract a large amount of pure water from high-salt wastewater, separate monovalent salt and divalent salt, extract divalent salt solid and realize zero emission of coking wastewater and effective recycling of resources.
The aim of the invention can be achieved by the following technical measures:
a high-salt wastewater thermal-vibration cyclone salt extraction system, comprising:
the softening pretreatment device comprises a high-salt wastewater inlet, a hard water outlet and a soft water outlet;
the hard water outlet is communicated with a water inlet of the 3-time concentrated SWRO reverse osmosis unit through a pipeline;
the 3-time concentrated SWRO reverse osmosis unit is internally provided with a SWRO reverse osmosis membrane, the pure water output end of the 3-time concentrated SWRO reverse osmosis unit is connected with the first pure water tank, and the concentrated water output end of the 3-time concentrated SWRO reverse osmosis unit is communicated with the water inlet of the thermal vibration cyclone evaporator through a pipeline;
the water outlet of the thermal vibration cyclone evaporator is communicated with the second pure water tank, and the salt outlet of the thermal vibration cyclone evaporator is connected with the solid salt tank;
the soft water outlet is connected with a 5-time concentrated NF component through a pipeline, the 5-time concentrated NF component comprises a water inlet tank, a filter, a water producing tank and a concentrated water tank, the input end of the water inlet tank is connected with the soft water outlet of the softening pretreatment equipment, the output end of the water inlet tank is connected with the input end of the filter through a fourth booster pump, an NF nanofiltration membrane is arranged in the filter, the water producing outlet of the filter is connected with the input end of the water producing tank, and the concentrated water outlet of the filter is connected with the input end of the concentrated water tank;
the output end of the water producing tank is communicated with the water inlet of the monovalent salt soft water tank through a pipeline;
the output end of the concentrated water tank is connected with the input end of a 2-time concentrated SWRO reverse osmosis unit through a pipeline, a SWRO reverse osmosis membrane is arranged in the 2-time concentrated SWRO reverse osmosis unit, the pure water output end of the 2-time concentrated SWRO reverse osmosis unit is communicated with a fourth pure water tank through a pipeline, and the concentrated water outlet of the 2-time concentrated SWRO reverse osmosis unit is communicated with softening pretreatment equipment through a pipeline;
the softening pretreatment device comprises a softening resin tank filled with softening resin.
Preferably, a first booster pump is arranged on a pipeline between the softening pretreatment device and the 3-time concentrated SWRO reverse osmosis unit.
Preferably, a second booster pump is arranged on a pipeline between the 3-time concentrated SWRO reverse osmosis unit and the thermal vibration cyclone evaporator.
Preferably, a third booster pump is arranged on a pipeline between the softening pretreatment device and the 5-time concentration NF component.
Preferably, a fifth booster pump is arranged on a pipeline between the water producing tank and the monovalent salt soft water tank.
Preferably, a sixth booster pump is arranged on a pipeline between the concentrate tank and the 2-time concentrated SWRO reverse osmosis unit.
Preferably, a seventh booster pump is arranged on a pipeline between the 2-time concentrated SWRO reverse osmosis unit and the softening pretreatment device.
The beneficial effects of the invention are as follows:
because the high-salt wastewater heat vibration cyclone salt extraction system provided by the scheme is divided into two paths from softening pretreatment equipment, one path comprises a 5-time concentration NF component, a 2-time concentration SWRO reverse osmosis unit and a monovalent salt soft water tank, and the other path comprises a 3-time concentration SWRO reverse osmosis unit and a heat vibration cyclone evaporator. The high-salt wastewater separates monovalent salt from divalent salt and high-valence salt through softening pretreatment equipment, and the monovalent salt enters a 5-time concentration NF component to flow back into a softening resin tank of the softening pretreatment equipment for continuous circulation treatment after a subsequent series of treatment as circulating regeneration liquid of the softening resin for recycling. The monovalent salt ions replace divalent salt and high-valence salt ions attached to the softening resin, the replaced divalent salt and high-valence salt enter a 3-time concentrated SWRO reverse osmosis unit for subsequent treatment, so that pure water meeting the standard is produced, and solid industrial divalent salt and high-valence salt are extracted through a thermosonic cyclone evaporator. And the monovalent salt supplemented by the total system can be removed along with soft water, so that the monovalent salt balance is achieved. Through the system, a large amount of pure water can be extracted from the high-salt wastewater, monovalent salt, divalent salt and high-valence salt are separated, divalent salt and high-valence salt solids can be extracted, and zero emission of coking wastewater and effective recycling of resources are realized.
The system adopts softening resin to separate monovalent salt from divalent salt and high-valence salt, the monovalent salt is circulated in the system only and is not treated, the monovalent salt overflowed from the whole system and the monovalent salt supplemented by waste water are balanced, and the divalent salt and the high-valence salt are extracted by adopting a thermal vibration cyclone evaporator. The core process of the process adopts the partial functions of softening resin, NF and SWRO, adjusts core parameters, balances monovalent salt, does not extract, adopts a thermal vibration cyclone evaporation process to extract divalent salt and high-valence salt, and solves the problems of high investment and operation blockage of the DTRO+MVR process.
Drawings
FIG. 1 is a schematic structural diagram of a high-salt wastewater thermal vibration cyclone salt extraction system provided by an embodiment of the invention;
FIG. 2 is a schematic diagram of a 5-fold concentrate NF assembly provided by an embodiment of the present invention;
fig. 3 is a front view of the thermoshocking cyclone evaporator provided in the present embodiment;
FIG. 4 is a cross-sectional view taken along the direction A-A in FIG. 3;
fig. 5 is a sectional view taken along the direction B-B in fig. 4.
In the figure:
1-softening pretreatment equipment; concentrating SWRO reverse osmosis unit 2-3 times; 3-a first pure water tank; 4-a thermal vibration cyclone evaporator; 5-a second pure water tank; 6-a solid salt box; concentrating NF components 7-5 times; 8-monovalent salt soft water tank; 11-2 times of concentrated SWRO reverse osmosis unit; 12-fourth pure water tank;
41-a drying chamber; 42-a heat source jacket; 43-rotating shaft; 44-paddles; 45-driving a motor;
411-a feed inlet; 412-a discharge port; 413-an air inlet;
421-a heat source inlet; 422-heat source outlet;
71-a water inlet tank; 72-a filter; 73-producing water tank; 74-concentrate tank.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in further detail with reference to the accompanying drawings and specific embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
In order that the present disclosure may be more fully described and fully understood, the following description is provided by way of illustration of embodiments and specific examples of the present invention; this is not the only form of practicing or implementing the invention as embodied. The description covers the features of the embodiments and the method steps and sequences for constructing and operating the embodiments. However, other embodiments may be utilized to achieve the same or equivalent functions and sequences of steps.
The high-salt wastewater thermal vibration cyclone salt extraction system according to the embodiment of the invention is shown in fig. 1 and comprises a softening pretreatment device 1, wherein the softening pretreatment device 1 comprises a water inlet for high-salt wastewater, a hard water outlet and a soft water outlet. The hard water outlet is communicated with a water inlet of the 3-time concentrated SWRO reverse osmosis unit 2 through a pipeline, and a first booster pump is arranged on the pipeline between the softening pretreatment equipment 1 and the 3-time concentrated SWRO reverse osmosis unit 2. The SWRO reverse osmosis unit 2 is internally provided with a SWRO reverse osmosis membrane, the pure water output end of the 3-time concentrated SWRO reverse osmosis unit 2 is connected with the first pure water tank 3, and the concentrated water output end of the 3-time concentrated SWRO reverse osmosis unit 2 is communicated with the water inlet of the thermal vibration cyclone evaporator 4 through a pipeline. The water outlet of the thermal vibration rotational flow evaporator 4 is communicated with a second pure water tank 5, and the salt outlet of the thermal vibration rotational flow evaporator 4 is connected with a solid salt tank 6. The pipelines of the 3-time concentrated SWRO reverse osmosis unit 2 and the thermal vibration cyclone evaporator 4 are provided with a second booster pump.
The soft water outlet is connected with the 5-time concentration NF component 7 through a pipeline, and a third booster pump is arranged on the pipeline between the softening pretreatment device 1 and the 5-time concentration NF component 7. The 5-fold concentrate NF assembly 7 includes a feed tank 71, a filter 72, a product tank 73, and a concentrate tank 74. The input end of the water inlet tank 71 is connected to the soft water outlet of the softening pretreatment device 1, and the output end of the water inlet tank 71 is connected to the input end of the filter 72 through the fourth booster pump. An NF nanofiltration membrane is arranged in the filter 72, a water producing outlet of the filter 72 is connected with an input end of the water producing tank 73, and a concentrated water outlet of the filter 72 is connected with an input end of the concentrated water tank 74. The output end of the water producing tank 73 is communicated with the water inlet of the monovalent salt soft water tank 8 through a pipeline. A fifth booster pump is arranged on the pipeline between the water producing tank 73 and the monovalent salt soft water tank 8. The output end of the concentrate tank 74 is connected with the input end of the 2-time concentrated SWRO reverse osmosis unit 11 through a pipeline, and the SWRO reverse osmosis membrane is arranged in the 2-time concentrated SWRO reverse osmosis unit 11. The pure water output end of the 2-time concentrated SWRO reverse osmosis unit 11 is communicated with the fourth pure water tank 12 through a pipeline, and the concentrated water outlet of the 2-time concentrated SWRO reverse osmosis unit 11 is communicated with the softening pretreatment device 1 through a pipeline. A sixth booster pump is arranged on the pipeline between the concentrate tank 74 and the 2-time concentrated SWRO reverse osmosis unit 11, and a seventh booster pump is arranged on the pipeline between the 2-time concentrated SWRO reverse osmosis unit 11 and the softening pretreatment device 1.
The softening pretreatment apparatus 1 includes a softening resin tank filled with a softening resin. Sodium ions are attached to the softening resin, when high-salt wastewater containing monovalent salt, divalent salt and high-valence salt enters the softening resin tank through the water inlet, the divalent and high-valence ions in the high-salt wastewater replace the sodium ions on the softening resin and are attached to the softening resin, the replaced sodium ions and the monovalent salt contained in the entering high-salt wastewater flow into the 5-time concentration NF component 7 through the soft water outlet in the solution, and the monovalent salt, the divalent salt and the high-valence salt in the solution are separated through the softening resin.
The filter 72 in the NF module 7 is 5 times concentrated to filter out most of the monovalent salt, and the monovalent salt replenished by the total system will follow the soft water out to reach monovalent salt balance. The remaining monovalent salt-containing solution cannot be used as a softened resin regeneration liquid because of insufficient concentration, so that the monovalent salt in the solution is concentrated 2-fold by the 2-fold concentration SWRO reverse osmosis unit 11, and the concentrated monovalent salt solution is returned to the softening pretreatment device 1 to be recycled as the softened resin regeneration liquid. As monovalent salts are insensitive to temperature, they are used as raw materials for monovalent salt regeneration in the system. After the monovalent salt returns to the softening pretreatment device 1, the sodium ions replace divalent salt and high-valence salt attached to the softening resin, and the divalent salt and the high-valence salt enter a thermal vibration rotational flow system from a hard water outlet to carry out salt extraction treatment. The whole system has the function of extracting bivalent salt and high-valence salt.
Specifically, the TDS in the high-salt wastewater flowing into the softening pretreatment device 1 was 3000mg/L, the flow was 100T/H, the monovalent salt content in the high-salt wastewater was 20%, and the divalent salt and high-valence salt content were 80%. Thus, the softening pretreatment device 1 is required to pretreat the high-salt wastewater with the aim of adding the total Cl to the high-salt wastewater - 、Na + Monovalent ions and Na 2+ 、SO 4 2- 、SO 3 2- And Ca 2 + 、Mg 2+ 、Al 2+ 、Fe 2+ Separation of bivalent ions and high-valence ions to obtain the Cl-containing material - 、Na + Nanofiltration filtrate with high ion concentration (yield of 100T/H) and Na-containing 2+ 、SO 4 2- 、SO 3 2- And Ca 2+ 、Mg 2+ 、Al 2+ 、Fe 2+ Nanofiltration concentrate with high concentration of divalent ions and high valence ions (the yield is 10T/H). And the macromolecular suspended matters are trapped, and heavy metal pollutants and most suspended matters in the wastewater are removed.
The softening resin can effectively intercept divalent ions and high-valence ions, such as Na 2+ 、SO 4 2- 、SO 3 2- And Ca 2+ 、Mg 2+ 、Al 2+ 、Fe 2+ And a divalent ion, wherein the divalent ion and the high-valence ion replace sodium ions attached to the softening resin. And replaced monovalent sodium ions and steel-supplemented monovalent salt ions (mainly Cl) - 、Na + ) Can effectively permeate through the softening resin and enter the 5-time concentrated NF component 7 through a soft water outlet. Softening resin against Na 2+ 、SO 4 2- 、SO 3 2- And Ca 2+ 、Mg 2+ 、Al 2+ 、Fe 2+ The removal rate of the bivalent ions and the high-valence ions is stabilized to be more than 99 percent.
The filter 72 in the 5-time concentrated NF module 7 carries out nanofiltration treatment on the inflow nanofiltration filtrate, and the produced water after nanofiltration treatment is mainly monovalent sodium chloride solution, also called soft brine, which firstly enters the water producing tank 73, and the soft brine in the water producing tank 73 flows into the monovalent salt soft water tank 8 through a pipeline. The flow rate of the nanofiltration filtrate entering the 5-time concentration NF component 7 is 100T/H, the yield of soft brine is 80T/H, wherein the Na in the soft brine is + The concentration was 600mg/L. The concentrated water after nanofiltration treatment enters a concentrated water tank 74, wherein the concentrated water is mainly monovalent sodium chloride, and the amount of the produced concentrated water is 20T/H, and the concentration of sodium ions is 1.5%.
Because the concentration of sodium ions in the concentrated water is 1.5%, the concentrated water cannot be used as a regeneration liquid of the softening resin, and the concentration of sodium ions is 3% only as a regeneration liquid of the softening resin, the concentrated water subjected to nanofiltration treatment enters a 2-time concentrated SWRO reverse osmosis unit 11 from a concentrated water tank 74, the 2-time concentrated SWRO reverse osmosis unit 11 carries out 2-time concentration treatment on the inflow concentrated water, and the concentrated water subjected to reverse osmosis desalination treatment by the 2-time concentrated SWRO reverse osmosis unit 11 is second-order produced water and second-order concentrated water. The second-order produced water (the amount of which is 10T/H) is pure water meeting the standard, and pollutants such as COD, bacteria, ammonia nitrogen and the like, chemical pollutants, radioactive substances, bacteria and the like in the water are removed, so that the second-order produced water flows into the fourth pure water tank 12 after being further purified, the purified second-order produced water is purified water meeting the zero emission standard, can be recycled, saves water resources, realizes resource utilization, and saves cost. And second-order concentrated water (the concentration of sodium ions reaches 3%) flows back into the softening resin tank of the softening pretreatment device 1 to serve as circulating regeneration liquid of the softening resin, and the circulating treatment is continued, so that the output of the second-order concentrated water is 10T/H. Sodium ions in the second-order concentrated water replace divalent and high-valence ions attached outside the softening resin, the replaced divalent and high-valence ions enter the solution to synthesize nanofiltration concentrated water, and the nanofiltration concentrated water enters the 3-time concentrated SWRO reverse osmosis unit 2 from a hard water outlet.
After the trapped nanofiltration concentrated water (the output of the trapped nanofiltration concentrated water is 10T/H) enters the 3-time concentration SWRO reverse osmosis unit 2 from a hard water outlet, the 3-time concentration SWRO reverse osmosis unit 2 carries out 3-time concentration treatment on the inflow nanofiltration concentrated water, and the nanofiltration concentrated water after the 3-time concentration SWRO reverse osmosis unit 2 reverse osmosis desalination treatment is divided into third-order produced water and third-order concentrated water. The third-order produced water (the amount of the third-order produced water is 6T/H) is pure water meeting the standard, pollutants such as COD, bacteria, ammonia nitrogen and the like, chemical pollutants, radioactive substances, bacteria and the like in the water are removed, so that the third-order produced water flows into the first pure water tank after being further purified, the purified first-order produced water is purified water, meets the zero emission standard, can be recycled, saves water resources, realizes resource utilization, and saves cost. The third-order concentrated water enters a thermal vibration cyclone evaporator 4, solid industrial bivalent salt and high-valence salt are extracted through the thermal vibration cyclone evaporator 4, the solid bivalent salt and the high-valence salt are put into a solid salt box 6, and the evaporated condensate flows to a second pure water box 5.
In this embodiment, the first booster pump, the second booster pump, the third booster pump, the fourth booster pump, the fifth booster pump, the sixth booster pump, and the seventh booster pump all function to pressurize the flowing liquid.
In this embodiment, the thermosonic cyclone evaporator 4 is preferably used to separate divalent and higher salts from the solution and extract pure water. As shown in fig. 3 to 5, the thermoshock evaporator 4 provided in this embodiment mainly comprises a drying chamber 41, a heat source jacket 42, a paddle 44, a rotating shaft 43, a feed inlet 411, a discharge outlet 412, an air inlet 413, a heat source inlet 421, a heat source outlet 422, and other structures.
The drying chamber 41 is of a hollow structure, one end of the drying chamber 41 is provided with a feed inlet 411 and an air inlet 413, and the other end is provided with a discharge outlet 412. High temperature process gas is introduced into the drying chamber 41 through the gas inlet 413. The inlet 413 for introducing the high-temperature process gas and the inlet 411 are arranged on the same side, so that the third-order concentrated water and the high-temperature process gas move in the dryer 1 in the same direction. The drying chamber 41 is preferably in a horizontal cylindrical structure, but is not limited thereto.
The heat source jacket 42 is disposed around the outside of the drying chamber 41, a high temperature medium as a heat source circulates in the heat source jacket 42, and a heat source outlet 422 and at least one heat source inlet 421 are disposed on the heat source jacket 42. The high temperature medium is preferably steam or heat transfer oil, but is not limited thereto.
The rotating shaft 43 is arranged at the middle position of the drying chamber 41 and penetrates through two ends of the drying chamber 41, namely, the rotating shaft 43 is coaxial with the drying chamber 41, and a driving motor 45 for driving the rotating shaft 43 to rotate is arranged on the outer side of the drying chamber 41.
The blade 44 is installed on the rotating shaft 43, in this scheme, two types of specially designed blades 44 are assembled on different positions of the rotating shaft 43, specifically, N groups of spreading blades are installed on a part, located at the feed inlet 411, of the rotating shaft 43, Q groups of spreading blades are installed on a part, located at the discharge outlet 412, of the rotating shaft 43, and M groups of transmission blades are installed on the middle part of the rotating shaft 43. Wherein N, Q, M is an integer greater than 1, and the specific number is determined according to the requirement. As a preferable scheme, the spreading blades and the transmission blades are respectively embedded into the rotating shaft 43, and the L rows of blades 44 are uniformly arranged in the circumferential radial direction of the cylinder body of the whole drying chamber 41. Wherein L is an integer greater than 1, and the specific amount is determined according to the need.
Specifically, the spreading blades are distributed at the feeding end and the discharging end of the rotating shaft 43, as a further preferable scheme, the N spreading blades are installed on each column of the part of the rotating shaft 43, which is located at the feeding port 411, the spreading blades are installed at a preset angle with the rotating shaft 43, and the purpose of installation is to realize that third-order concentrated water is immediately spread on the surface of the hot wall after entering the drying chamber 41 and has the function of conveying to the discharging end. Q spreading paddles are arranged on each column of the part of the rotating shaft 43, which is positioned at the discharge hole 412, wherein the spreading paddles are arranged at an oblique reverse angle with the spreading paddles of the feed inlet 411, namely, the installation angles of the two are opposite, and the purpose of the installation is to buffer the inertial force of the product during discharge to achieve the function of free gravity discharge.
In this embodiment, as a further preferable aspect, the spreading blade and the transmission blade are fixedly connected to the rotating shaft 43 by bolts, respectively. The assembly mode ensures that the installation and adjustment of the spreading blades and the transmission blades are more flexible, and ensures that the thermal vibration cyclone evaporator 4 can adapt to different dried substances and the change of the treatment capacity.
In this embodiment, as a preferable scheme, the surfaces of the spreading blade and the conveying blade are both plated with wear-resistant materials.
In this embodiment, the distance H between the end of the spreading blade or the transmission blade away from the rotating shaft 43 and the inner wall of the drying chamber 41 has an influence on the drying process, taking the values of the distance H as 2mm and 5mm as examples, the eddy effect of the flow field in the heat vibration cyclone evaporator 4 with the distance of 2mm is strong, and the third-order concentrated water moves closer to the wall surface, so that the mixed heat transfer effect is good. In this embodiment, the distance between the end of the spreading blade far away from the rotating shaft 43 and the inner wall of the drying chamber 41 is preferably 2-10 mm. Similarly, the distance between the end of the transmission blade far away from the rotating shaft 43 and the inner wall of the drying chamber 41 is 2-10 mm.
In this embodiment, the influence of the installation angle between the spreading blades and the rotating shaft and the influence of the installation angle between the transmission blades and the rotating shaft on the drying process are analyzed, the included angle between the N groups of spreading blades positioned at the front section of the rotating shaft 43 and the rotating shaft 43 is set to 15 degrees, the included angle between the M groups of transmission blades positioned at the middle section of the rotating shaft 43 and the rotating shaft 43 is set to-45 degrees, the included angle between the Q groups of spreading blades positioned at the rear section of the rotating shaft 43 and the rotating shaft 43 is set to-75 degrees, and the influence of the installation angle between the blades 44 and the rotating shaft 43 on the drying process is analyzed, so that the spreading blades with a large installation angle of the discharge port 412 are beneficial to the stable discharge of the dryer, and the transmission blades at the middle section are the main working area of the drying process and play a leading role in the drying process of divalent salt in third-order concentrated water. Therefore, as a preferable scheme, N groups of spreading blades positioned at the front section of the rotating shaft 43 are set as inlet spreading groups, wherein the included angle between the spreading blades and the rotating shaft 43 is preferably 10-20 degrees; the Q groups of spreading blades positioned at the rear section of the rotating shaft 43 are arranged as outlet material receiving groups, wherein the included angle between the spreading blades and the rotating shaft 43 is preferably 70-80 degrees; the M groups of transmission paddles positioned at the middle section of the rotating shaft 43 are set as middle transmission groups, wherein the included angle between the transmission paddles and the rotating shaft 43 is preferably 40-50 degrees.
In the embodiment, the influence of single installation angles of three paddles 44 of 30 degrees, 45 degrees and 60 degrees on the drying process is analyzed, the optimal installation angle of the paddles 44 is 45 degrees, under the condition, smooth material transportation can be realized, the material temperature of the discharge port 412 is 440K, and the water content of the material of the discharge port 112 can be reduced to 20%. Therefore, as another preferable scheme, the included angle between the spreading blade and the rotating shaft 43 is 40-50 degrees, and the included angle between the transmission blade and the rotating shaft 43 is 40-50 degrees.
In this embodiment, the other air inlets 413 of the thermosonic cyclone evaporator 4 are set to be negative pressure, so that the air can enter the drying chamber 41, and the pressure at the tail ends of the paddles 44 is the maximum, so that the best position for the mixed heat transfer effect in the thermosonic cyclone evaporator 4 is obtained.
When the thermal vibration cyclone evaporator 4 provided by the scheme works, the rotating shaft 43 is driven by the driving motor 45 outside the drying chamber 41, so that the paddles 44 are driven to rotate at a high speed, and strong vortex is formed in the drying chamber 41. After entering the drying chamber 41, third-order concentrated water is centrifugally distributed on the surface of the heating wall in the drying chamber 41 by the vortex action to form a continuous thin high-turbulence concentrated water thin layer, the thin layer moves spirally from the feed inlet 411 to the discharge outlet 412 at a certain speed under the assistance of process gas, and in the process, the concentrated water thin layer continuously collides with the heating wall in the drying chamber 41 for heat transfer, so as to finish the processes of contact, reaction, sterilization or drying and the like. Meanwhile, a certain amount of preheated high-temperature process gas which is consistent with the movement direction of the materials can be adopted in the process, the process forms a combined action with high-speed vortex in the drying chamber 41 to push the concentrated water thin layer to do spiral movement along the inner wall to the outlet direction, the concentrated water thin layer realizes strong heat convection heat exchange under the repeated wrapping, carrying and flowing of the process gas, the moisture in the concentrated water is evaporated to become water vapor, the water vapor enters the second pure water tank 5 to become purified water, and the residual divalent salt and high-valence salt enter the solid salt tank 6 after being evaporated to dryness. The residence time of the concentrated water thin layer in the turbine thin layer thermal vibration cyclone evaporator 4 is short, start-stop and emptying can be realized rapidly, and the drying equipment is simple to operate and convenient to adjust and control.
The high-temperature medium and the preheated process gas are used as heat sources to respectively conduct heat conduction and heat convection processes with third-order concentrated water, so that a coupling drying effect is realized. The heat source jacket 42 of the drying chamber 41 is filled with a high-temperature medium, so that the inner wall of the drying chamber 41 is uniformly and effectively heated, and the heat source jacket 42 continuously provides the high-temperature medium to ensure high-strength heat transfer. The high-strength vortex hot air formed by the high-speed rotating blades 44 can rapidly dry substances far away from the heating wall surface in the thermal vibration cyclone evaporator 4 in a thermal convection mode while conveying concentrated water.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.
Claims (7)
1. A high-salt wastewater thermal vibration cyclone salt extraction system, comprising:
the softening pretreatment device comprises a high-salt wastewater inlet, a hard water outlet and a soft water outlet;
the hard water outlet is communicated with a water inlet of the 3-time concentrated SWRO reverse osmosis unit through a pipeline;
the 3-time concentrated SWRO reverse osmosis unit is internally provided with a SWRO reverse osmosis membrane, the pure water output end of the 3-time concentrated SWRO reverse osmosis unit is connected with the first pure water tank, and the concentrated water output end of the 3-time concentrated SWRO reverse osmosis unit is communicated with the water inlet of the thermal vibration cyclone evaporator through a pipeline;
the water outlet of the thermal vibration cyclone evaporator is communicated with the second pure water tank, and the salt outlet of the thermal vibration cyclone evaporator is connected with the solid salt tank;
the soft water outlet is connected with a 5-time concentrated NF component through a pipeline, the 5-time concentrated NF component comprises a water inlet tank, a filter, a water producing tank and a concentrated water tank, the input end of the water inlet tank is connected with the soft water outlet of the softening pretreatment equipment, the output end of the water inlet tank is connected with the input end of the filter through a fourth booster pump, an NF nanofiltration membrane is arranged in the filter, the water producing outlet of the filter is connected with the input end of the water producing tank, and the concentrated water outlet of the filter is connected with the input end of the concentrated water tank;
the output end of the water producing tank is communicated with the water inlet of the monovalent salt soft water tank through a pipeline;
the output end of the concentrated water tank is connected with the input end of a 2-time concentrated SWRO reverse osmosis unit through a pipeline, a SWRO reverse osmosis membrane is arranged in the 2-time concentrated SWRO reverse osmosis unit, the pure water output end of the 2-time concentrated SWRO reverse osmosis unit is communicated with a fourth pure water tank through a pipeline, and the concentrated water outlet of the 2-time concentrated SWRO reverse osmosis unit is communicated with softening pretreatment equipment through a pipeline;
the softening pretreatment device comprises a softening resin tank, wherein the softening resin tank is filled with softening resin;
when the high-salt wastewater containing monovalent salt, divalent salt and high-valence salt enters the softening resin tank through the water inlet, the divalent and high-valence ions in the high-salt wastewater replace sodium ions on the softening resin and are attached to the softening resin, the replaced sodium ions and the monovalent salt contained in the entering high-salt wastewater flow into the 5-time concentration NF component through the soft water outlet in the solution, and the monovalent salt, the divalent salt and the high-valence salt in the solution are separated through the softening resin;
the monovalent salt in the solution is concentrated by 2 times through a 2-time concentrated SWRO reverse osmosis unit, the concentrated monovalent salt solution is returned to softening pretreatment equipment to be used as a softened resin regeneration solution, and the divalent salt and the high-valence salt enter a thermal vibration rotational flow system from a hard water outlet to carry out salt extraction treatment;
the thermal vibration cyclone evaporator comprises a drying chamber, a heat source jacket, paddles, a rotating shaft, a feed inlet, a discharge outlet, an air inlet, a heat source inlet and a heat source outlet.
2. The high-salinity wastewater heat-vibration cyclone salt extraction system according to claim 1, wherein a first booster pump is arranged on a pipeline between the softening pretreatment device and the 3-time concentrated SWRO reverse osmosis unit.
3. The high-salinity wastewater heat-vibration cyclone salt extraction system according to claim 1, wherein a second booster pump is arranged on a pipeline between the 3-time concentration SWRO reverse osmosis unit and the heat-vibration cyclone evaporator.
4. The high salt wastewater thermal vibration cyclone salt extraction system according to claim 1, wherein a third booster pump is arranged on a pipeline between the softening pretreatment device and the 5-time concentration NF component.
5. The high-salt wastewater thermal vibration cyclone salt extraction system according to claim 1, wherein a fifth booster pump is arranged on a pipeline between the water production tank and the monovalent salt soft water tank.
6. The high-salt wastewater thermal vibration cyclone salt extraction system according to claim 1, wherein a sixth booster pump is arranged on a pipeline between the concentrated water tank and the 2-time concentrated SWRO reverse osmosis unit.
7. The high-salinity wastewater thermal vibration cyclone salt extraction system according to claim 1, wherein a seventh booster pump is arranged on a pipeline between the 2-time concentration SWRO reverse osmosis unit and the softening pretreatment device.
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| EP3598871A4 (en) * | 2017-02-07 | 2021-05-12 | Sylvan Source Inc. | Water treatment and desalination |
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| CN104692574A (en) * | 2014-12-22 | 2015-06-10 | 内蒙古久科康瑞环保科技有限公司 | Treatment method of high saline wastewater |
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