CN211226645U - Coupling flue gas purification handles contains salt effluent disposal system - Google Patents
Coupling flue gas purification handles contains salt effluent disposal system Download PDFInfo
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- CN211226645U CN211226645U CN201921416443.3U CN201921416443U CN211226645U CN 211226645 U CN211226645 U CN 211226645U CN 201921416443 U CN201921416443 U CN 201921416443U CN 211226645 U CN211226645 U CN 211226645U
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Abstract
The utility model discloses a low-energy-consumption high-salt-content wastewater treatment system, which comprises a raw water tank and a flue gas purification liquid storage tank, wherein the raw water tank is connected to the feed liquid side of a forward osmosis membrane component through a pipeline, the outlet of the flue gas purification liquid storage tank is connected with a liquid drawing tank, the outlet of the liquid drawing tank is connected to the liquid drawing inlet of the forward osmosis membrane component through a pipeline, and a liquid drawing pump is arranged on the pipeline; and a drawing liquid outlet of the forward osmosis membrane module is connected to a flue gas purification and absorption device. The system is utilized to treat wastewater, and the wastewater enters a rear-end concentrated water treatment device after being concentrated to a set concentration; meanwhile, the drawing liquid is diluted to a set concentration and then is used as the flue gas purification absorption liquid to be sent to a flue gas purification absorption device, and the diluted drawing liquid is directly used as the absorption liquid; the water in the absorption wastewater of the absorption liquid is used for flue gas purification, so that the water supplement amount of the flue gas purification absorption device is reduced, and the high-energy-consumption regeneration process is avoided.
Description
Technical Field
The utility model belongs to the technical field of waste water treatment, concretely relates to coupling gas cleaning handles contain salt effluent disposal system.
Background
The salt-containing wastewater has wide generation ways, the water quantity is increased year by year, and the salt-containing wastewater accounts for a large proportion in the total discharge amount of the chemical wastewater. The method is always recognized to be highly difficult to treat the wastewater due to the characteristics of large discharge and complex water quality. Such waste water contains a large amount of inorganic salts such as Cl in addition to organic contaminants-、SO4 2-、Na+、Ca2+Plasma, representative wastewater includes mine water, coal gas washing wastewater, desalted water system drainage, reuse water system drainage concentrated water, shale gas and coal bed gas mining wastewater, pharmaceutical wastewater, printing and dyeing wastewater, oil field wastewater and the like. If the salt-containing wastewater is directly discharged into a water body, aquatic organisms, domestic water and industrial and agricultural water can be influenced, and harm to different degrees is caused. The prior method for treating the salt-containing wastewater mainly comprises reverse osmosis, multi-effect evaporative crystallization, mechanical thermal compression, electrodialysis and the combination of the above methods. At present, the most widely applied method for treating salt-containing wastewater is reverse osmosis, but the concentration rate is limited, and the problems of serious membrane pollution, high external high pressure energy consumption and the like exist in the treatment process; the methods such as multiple-effect evaporative crystallization, mechanical evaporative crystallization and the like belong to a thermal separation method, and have the problems of high equipment investment and treatment cost and the like; the electrodialysis has low desalting rate and desalting effectLow rate and the like.
Forward Osmosis (Forward Osmosis) is a membrane separation process driven by osmotic pressure, and water spontaneously diffuses through a Forward Osmosis membrane from the higher water chemical potential side (low osmotic pressure side) to the lower water chemical potential side (high osmotic pressure side) without the need for external pressure. The waste water is treated by utilizing a forward osmosis technology, salt and other pollutants in the waste water are intercepted by a forward osmosis membrane, the waste water enters a side of an extraction liquid (high osmotic pressure) to be concentrated, and the extraction liquid is diluted at the same time. The forward osmosis technology has the advantages of no need of external high pressure in the membrane separation process, low energy consumption, low requirement on the strength of membrane materials, difficult occurrence of membrane pollution and long service life of the membrane. In addition, the pretreatment requirement is lower compared with reverse osmosis.
The forward osmosis technology is not used on a large scale at present, and one of the main limiting reasons is high energy consumption for concentrating and regenerating the draw solution. The currently industrially used draw solution is composed of NH3And CO2Reacting water-soluble ammonium bicarbonate solution with high osmotic pressure, which is heated to 60 deg.C and decomposed to form NH3And CO2Thereby achieving regeneration. But the heating energy consumption is high, and in addition, the ammonia dissolved in water can influence the water quality of the produced water. The patent document CN104803448A discloses a "forward osmosis treatment method for wastewater with high salinity organic concentration" which uses multi-effect evaporation technology to concentrate the diluted driving liquid, and the concentration process consumes steam and the cost is not necessarily low. The 'continuously operable circulating forward osmosis high-salt organic wastewater treatment system' disclosed in the patent document with the publication number of CN106422780 adopts a reverse osmosis technology to concentrate the draw solution, but the reverse osmosis concentration rate is limited, the concentration of the concentrated draw solution is not particularly high, the spontaneous flow of the water in the forward osmosis system is required to be maintained, and the osmotic pressure of the wastewater to be treated is required to be less than that of the draw solution, so that the system is not suitable for treating the concentrated water with high salt content. The forward osmosis membrane separation process has advantages, but the absorption solution concentration regeneration energy consumption is high, and when the forward osmosis technology is applied to treat saline wastewater, a proper absorption solution needs to be selected, so that the problem to be solved is to develop a regeneration mode with low energy consumption or a wastewater treatment system directly utilizing the diluted absorption solution.
Disclosure of Invention
In order to solve the problem, the utility model provides a coupling gas cleaning handles contain salt effluent disposal system can realize containing the low energy consumption of salt waste water simultaneously and handle and the gas cleaning system moisturizing.
In order to achieve the purpose, the utility model relates to a saliferous waste water treatment system with coupled flue gas purification treatment, which comprises a raw water tank and a flue gas purification liquid storage tank, wherein the raw water tank is connected to the feed liquid side of a forward osmosis membrane component through a pipeline, the outlet of the flue gas purification liquid storage tank is connected with a drawing liquid tank, the outlet of the drawing liquid tank is connected to the drawing liquid inlet of the forward osmosis membrane component through a pipeline, and a drawing liquid pump is arranged on the pipeline; and a drawing liquid outlet of the forward osmosis membrane component is connected to the flue gas purification and absorption device.
Further, the entrance of former pond is connected with pretreatment systems, and pretreatment systems includes coagulating tank and filter, and coagulating tank, filter and former pond connect gradually.
Furthermore, a raw water pump is arranged between the coagulation tank and the filter.
Further, the liquid outlet that draws of the liquid side that draws of forward osmosis membrane subassembly passes through the pipe connection with the entry that draws the liquid pond, is provided with on the pipeline and draws liquid circulation valve.
Furthermore, a concentrated water valve is arranged between the inlet side outlet of the forward osmosis membrane component and the raw water pool, the concentrated water valve is a three-way valve, the inlet of the concentrated water valve is connected with the inlet side outlet of the forward osmosis membrane component, the first outlet of the concentrated water valve is connected with the inlet of a concentrated water treatment device, and the second outlet of the concentrated water valve is connected with the raw water pool.
Furthermore, the concentrated water treatment device is an evaporative crystallization device.
Further, the flue gas purification and absorption device is a wet desulphurization device, a wet denitration device and/or a wet decarburization device.
Compared with the prior art, the utility model discloses following profitable technological effect has at least:
a salt-containing wastewater treatment system coupled with flue gas purification treatment is characterized in that a wastewater outlet is connected to the feed side of a forward osmosis membrane module through a pipeline, a flue gas purification liquid storage tank is connected with the liquid suction side of the forward osmosis membrane module through a pipeline, and the wastewater enters a rear-end concentrated water treatment device after being concentrated to a set concentration; meanwhile, the drawing liquid is diluted to a set concentration and then is used as the flue gas purification absorption liquid to be sent to a flue gas purification absorption device, and the diluted drawing liquid is directly used as the absorption liquid; the treatment of the salt-containing wastewater based on forward osmosis coupling flue gas purification is realized; compared with the traditional recovery absorption liquid, the energy consumption is greatly reduced, and meanwhile, the absorption liquid absorbs water in the wastewater for flue gas purification, so that the water supplement amount of the flue gas purification absorption device is reduced, and the high-energy-consumption regeneration process is avoided.
By adopting the treatment system, the forward osmosis technology is adopted to realize the concentration of the saline water, the energy consumption is low, the treatment cost is low, and the membrane pollution is small; the forward osmosis treatment system maintains higher osmotic pressure difference, the concentration rate is high, the salt content of the generated concentrated water is high, the water quantity is small, and the scale of the matched evaporative crystallization device can be reduced.
Drawings
FIG. 1 is a schematic view of the high-salinity wastewater treatment process of the present invention.
In the drawings: 1-a coagulation tank, 2-a raw water pump, 3-a filter, 4-a raw water tank, 5-a feed liquid pump, 6-a forward osmosis membrane component, 7-a concentrated water valve, 8-a flue gas purification liquid storage tank, 9-a flue gas purification liquid pump, 10-a drawing liquid tank, 11-a drawing liquid pump, 12-a drawing liquid circulation valve and 13-a drawing liquid dilution liquid valve.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings and specific embodiments.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are used merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention. Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified. In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
A salt-containing wastewater treatment process system coupled with flue gas purification treatment comprises a pretreatment system, a drawing liquid preparation system, a membrane treatment system and a drawing liquid recycling system. The pretreatment system comprises a coagulation tank 1, a raw water pump 2 and a filter 3; the drawing liquid preparation system comprises a flue gas purification liquid storage tank 8 and a flue gas purification liquid pump 9, and the membrane treatment system comprises a raw water tank 4, a feeding liquid pump 5, a forward osmosis membrane assembly 6 and a concentrated water valve 7; the drawing liquid recycling system comprises a drawing liquid pool 10, a drawing liquid pump 11, a drawing liquid circulating valve 12 and a drawing liquid diluent valve 13.
Referring to fig. 1, a salt-containing wastewater treatment system coupled with flue gas purification treatment comprises a coagulation tank 1, a forward osmosis membrane assembly 6 and a flue gas purification liquid storage tank 8, wherein an outlet of the coagulation tank 1 is sequentially connected with a raw water pump 2, a filter 3, a raw water pool 4 and a feed liquid pump 5, and the feed liquid pump 5 is connected to a feed liquid side inlet of the forward osmosis membrane assembly 6 through a pipeline; a feed liquid side outlet of the forward osmosis membrane component 6 is connected with the raw water tank 4, a concentrated water valve 7 is arranged between the feed liquid side outlet of the forward osmosis membrane component 6 and the raw water tank 4, the concentrated water valve 7 is a three-way valve, an inlet of the concentrated water valve 7 is connected with the feed liquid side outlet of the forward osmosis membrane component 6, a first outlet of the concentrated water valve 7 is connected with an inlet of a concentrated water treatment device, and a second outlet of the concentrated water valve 7 is connected with the raw water tank 4; an outlet of the flue gas purification liquid storage tank 8 is sequentially connected with a flue gas purification liquid pump 9, a liquid drawing pool 10 and a liquid drawing pump 11, and an outlet of the liquid drawing pump 11 is connected to a liquid drawing inlet on a liquid drawing side of the forward osmosis membrane assembly 6 through a pipeline; the drawing liquid on the drawing liquid side of the forward osmosis membrane assembly 6 is provided with two outlets, one outlet is connected with the inlet of the drawing liquid pool 10 through a pipeline, and the pipeline is provided with a drawing liquid circulating valve 12; and the other outlet is sent to a flue gas purification and absorption device.
The process for treating the salt-containing wastewater by utilizing the salt-containing wastewater treatment system coupled with the flue gas purification treatment comprises the following steps of:
(1) the flue gas purification absorption liquid comprises an absorbent used in the processes of wet desulphurization, wet denitration and wet decarburization, and enters a liquid drawing pool through a liquid drawing reserve pump;
(2) the salt-containing wastewater from an upstream device is treated by adopting different pretreatment processes according to different wastewater qualities. The pretreatment step comprises the following steps: coagulating sedimentation and filtering. The coagulation sedimentation reduces macromolecular pollutants in water to be treated by adding lime-soda ash, reduces the hardness of wastewater, and prevents the membrane component from being blocked by the pollutants; the filtration comprises multi-medium filtration, security filtration, microfiltration membrane filtration and ultrafiltration membrane filtration, and one or more of the filtration is selected according to the water quality characteristics; the pretreated wastewater enters a raw water pool;
(3) the raw water in the forward osmosis raw water pool passes through a feed liquid pump and is pumped into a feed liquid side of the forward osmosis membrane component to flow in a circulating manner; meanwhile, pumping the draw solution in the draw solution pool to the draw solution side of the forward osmosis membrane assembly through a draw solution pump to serve as forward osmosis draw solution to flow circularly;
(4) because the osmotic pressure difference between the feed liquid side and the draw liquid side of the forward osmosis membrane component, water in the raw water tank enters the draw liquid side through the forward osmosis membrane component, salt and other pollutants are intercepted, the TDS (total dissolved solids) in the feed liquid increases along with concentration, when the TDS is concentrated to be larger than or equal to 120000mg/L at most, the feed liquid is discharged through a concentration valve and is sent to a back-stage concentrated water treatment device, and the concentrated water treatment device is an evaporative crystallization device.
(5) The water in the absorption raw water of the drawing liquid is diluted, and when the concentration of the drawing liquid is diluted to the concentration of the absorption liquid when the flue gas purification and absorption device works, the drawing liquid is discharged through a valve and then is sent to the flue gas purification and absorption device; and pumping the liquid in the flue gas purification liquid storage tank into a liquid pumping pool for supplement.
The salt-containing wastewater comprises mine water, shale gas and coal bed gas mining wastewater, chemical wastewater subjected to advanced treatment, concentrated water discharged by a reverse osmosis device, landfill leachate, brackish water, oil field wastewater and the like.
The method comprises the following steps of (1) carrying out wastewater treatment by utilizing a saline wastewater treatment system based on forward osmosis coupling flue gas purification, combining flue gas purification and forward osmosis, taking a flue gas purification absorption liquid as an extraction liquid, enabling water in the wastewater to spontaneously flow to an extraction liquid side due to osmotic pressure difference, intercepting salt and pollutants by a forward osmosis membrane to realize wastewater concentration, and enabling the wastewater to enter a rear-end concentrated water treatment device after the wastewater is concentrated to a set concentration; meanwhile, the drawing liquid is diluted to a set concentration and then is sent to a flue gas purification and absorption device as a flue gas purification absorbent, and the diluted drawing liquid is not concentrated, recovered and regenerated, but directly used as an absorption liquid; compared with the traditional recovery absorption liquid, the energy consumption is greatly reduced, and meanwhile, the absorption liquid absorbs water in the wastewater for flue gas purification, so that the water supplement amount of the flue gas purification absorption device is reduced, and the high-energy-consumption regeneration process is avoided. Can realize the low energy consumption of the salt-containing wastewater to process and the water supplement of the flue gas purification and absorption device at the same time, and has obvious economical efficiency and operability.
The following describes different waste water treatment processes
Example 1
Adopt above-mentioned system to handle printing and dyeing wastewater through advanced treatment, the quality of water characteristic is:
the method comprises the following steps: liquid ammonia in the flue gas purification liquid storage tank 8 enters the liquid drawing pool 10 through the pump 9 to be used as drawing liquid for standby. Printing and dyeing wastewater enters a coagulation tank 1, lime-sodium carbonate is added, then the mixture enters a filter 3 through a pump 2, the filter 3 is a multi-media filter, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in the wastewater are removed and then the mixture enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Driven by osmotic pressure difference, water molecules in raw water enter the positive osmosis liquid drawing side through the positive osmosis membrane assembly 6, and liquid ammonia is diluted while the raw water is concentrated. When the TDS of the concentrated water after forward osmosis concentration is 300000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporation crystallization unit. When the concentration of the diluted ammonia water is 30%, the diluted ammonia water is discharged through a draw solution diluent valve 13 and then is sent to a desulfurizing tower to be used as an absorption liquid.
The treated wastewater is sent into an ammonia desulfurization tower to produce Ca2+<50mg/L,Mg2+<1.22mg/L, hardness<2mmol/L，Cl-<20mg/L,Al<10. mu.g/L, organic matter<2mg/L, which meets the water quality requirement of the process water for ammonia desulphurization engineering.
Example 2
Adopt above-mentioned system to handle the concentrated water of reuse water system external drainage, its quality of water characteristics is:
the method comprises the following steps: liquid ammonia in the flue gas purifying liquid storage tank enters a liquid drawing pool 10 through a pump 9 for standby. Concentrated water discharged from the reuse water system enters a coagulation tank 1, lime-sodium carbonate is added, then the concentrated water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the concentrated water is used as raw water to enter a raw water tank 4. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Under the driving of osmotic pressure difference, raw water enters the positive osmosis liquid drawing side through the positive osmosis membrane assembly 6, and liquid ammonia is diluted while the raw water is concentrated. When the TDS of the concentrated water after forward osmosis concentration is 200000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporation crystallization unit. When the concentration of the diluted ammonia water is 25%, the diluted ammonia water is discharged through a valve 13 and then is sent to a desulfurizing tower to be used as an absorption liquid.
The treated wastewater is sent into an ammonia desulfurization tower to produce Ca2+<50mg/L,Mg2+<1.22mg/L, hardness<2mmol/L，Cl-<20mg/L,Al<10. mu.g/L, organic matter<2mg/L, which meets the water quality requirement of the process water for ammonia desulphurization engineering.
Example 3
The mine water is treated by adopting the system, and the water quality is characterized in that:
liquid ammonia in the flue gas purifying liquid storage tank enters a liquid drawing pool 10 through a pump 9 for standby. Mine water enters a coagulation tank 1, lime-sodium carbonate is added, then the mine water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the mine water enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Driven by osmotic pressure difference, the concentrated water discharged from the recycling system enters the forward osmosis liquid-drawing side through the forward osmosis membrane assembly 6, and is diluted by liquid ammonia while being concentrated. When the TDS of the concentrated water after forward osmosis concentration is 200000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporation crystallization unit. When the concentration of the diluted ammonia water is 20%, the diluted ammonia water is discharged through a valve 13 and then is sent to a desulfurizing tower to be used as an absorption liquid. The treated wastewater is sent into an ammonia desulfurization tower to produce Ca2+<50mg/L,Mg2+<1.22mg/L, hardness<2mmol/L，Cl-<20mg/L,Al<10. mu.g/L, organic matter<2mg/L, which meets the water quality requirement of the process water for ammonia desulphurization engineering.
Example 4
The mine water is treated by adopting the system, and the water quality is characterized in that:
the concentrated urea solution in the flue gas purification solution storage tank enters the liquid drawing pool 10 through the pump 9 for standby. Mine water enters a coagulation tank 1, lime-sodium carbonate is added, then the mine water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the mine water enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Under the driving of osmotic pressure difference, the concentrated water discharged from the recycling system enters the side of the forward osmosis liquid drawing through the forward osmosis membrane component 6, and is concentrated while the concentrated urea solution is diluted. When the TDS of the concentrated water after forward osmosis concentration is 180000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporative crystallization unit. When the diluted urea concentration is 10%, the urea is discharged through a valve 13 and sent to a denitration device to be used as an absorption liquid.
Example 5
Adopt above-mentioned system to handle printing and dyeing wastewater through advanced treatment, the quality of water characteristic is:
the method comprises the following steps: and the ethanolamine concentrated solution in the flue gas purification solution storage tank enters a liquid drawing pool 10 through a pump 9 for standby. Printing and dyeing wastewater enters a coagulation tank 1, lime-sodium carbonate is added, then the mixture enters a filter 3 through a pump 2, the filter 3 is a multi-media filter, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in the wastewater are removed and then the mixture is used as raw water to enter a raw water pool 4. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Driven by osmotic pressure difference, the printing and dyeing wastewater enters the forward osmosis liquid drawing side through the forward osmosis membrane assembly 6, and is concentrated while the ethanolamine concentrated solution is diluted. When the TDS of the concentrated water after forward osmosis concentration is 280000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporative crystallization unit. When the diluted ethanolamine concentration is 30%, the diluted ethanolamine is discharged through a valve 13 and sent to a wet decarburization device to be used as an absorption liquid.
Example 6
The mine water is treated by adopting the system, and the water quality is characterized in that:
and the ethanolamine concentrated solution in the flue gas purification solution storage tank enters a liquid drawing pool 10 through a pump 9 for standby. Mine water enters a coagulation tank 1, lime-sodium carbonate is added, then the mine water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the mine water enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Under the driving of osmotic pressure difference, the concentrated water discharged from the recycling system enters the side of the forward osmosis drawing liquid through the forward osmosis membrane component 6, and is concentrated while the ethanolamine concentrated solution is diluted. When the TDS of the concentrated water after forward osmosis concentration is 150000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporative crystallization unit. When the diluted ethanolamine concentration is 20%, the diluted ethanolamine is discharged through a valve 13 and sent to a wet decarburization device to be used as an absorption liquid.
Example 7
The mine water is treated by adopting the system, and the water quality is characterized in that:
and the concentrated sodium citrate solution in the flue gas purification solution storage tank enters a liquid drawing pool 10 through a pump 9 for standby. Mine water enters a coagulation tank 1, lime-sodium carbonate is added, then the mine water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the mine water enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Driven by osmotic pressure difference, the concentrated water discharged from the recycling system enters the side of the forward osmosis liquid drawing through the forward osmosis membrane assembly 6, and is concentrated while the concentrated sodium citrate is diluted. When the TDS of the concentrated water after forward osmosis concentration is 200000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporation crystallization unit. When the concentration of the diluted sodium citrate absorption liquid is 20%, the diluted sodium citrate absorption liquid is discharged through a valve 13 and then is sent to a desulfurizing tower to be used as the absorption liquid.
Example 8
The mine water is treated by adopting the system, and the water quality is characterized in that:
the concentrated sodium hydroxide solution in the flue gas purifying solution storage tank enters the liquid drawing pool 10 through the pump 9 for standby. Mine water enters a coagulation tank 1, lime-sodium carbonate is added, then the mine water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the mine water enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Driven by osmotic pressure difference, the discharged concentrated water of the recycling system enters the side of the forward osmosis liquid drawing through the forward osmosis membrane assembly 6, and is concentrated while the concentrated sodium hydroxide solution is diluted. When the TDS of the concentrated water after forward osmosis concentration is 200000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporation crystallization unit. When the concentration of the diluted sodium hydroxide absorption liquid is 20%, the diluted sodium hydroxide absorption liquid is discharged through a valve 13 and then sent to a desulfurizing tower to be used as the absorption liquid.
Example 9
The mine water is treated by adopting the system, and the water quality is characterized in that:
the concentrated sodium sulfite solution in the flue gas purification solution storage tank enters a liquid drawing pool 10 through a pump 9 for standby. Mine water enters a coagulation tank 1, lime-sodium carbonate is added, then the mine water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the mine water enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Driven by osmotic pressure difference, the discharged concentrated water of the recycling system enters the forward osmosis liquid drawing side through the forward osmosis membrane assembly 6, and is concentrated while the concentrated sodium sulfite solution is diluted. When the TDS of the concentrated water after forward osmosis concentration is 150000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporative crystallization unit. When the concentration of the diluted sodium sulfite absorption solution is 20%, the solution is discharged through a valve 13 and sent to a denitration device to be used as the absorption solution.
Example 10
The mine water is treated by adopting the system, and the water quality is characterized in that:
and (3) enabling the methyldiethanolamine concentrated solution in the flue gas purification solution storage tank to enter a liquid drawing pool 10 through a pump 9 for standby. Mine water enters a coagulation tank 1, lime-sodium carbonate is added, then the mine water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the mine water enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Driven by osmotic pressure difference, the discharged concentrated water of the recycling system enters the side of the forward osmosis drawing liquid through the forward osmosis membrane assembly 6, and is concentrated while the methyldiethanolamine concentrated liquid is diluted. When the TDS of the concentrated water after forward osmosis concentration is 150000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporative crystallization unit. When the concentration of the diluted methyldiethanolamine is 20%, the diluted methyldiethanolamine is discharged through a valve 13 and then sent to a wet decarburization device to be used as absorption liquid.
Example 11
The mine water is treated by adopting the system, and the water quality is characterized in that:
and the triethanolamine concentrated solution in the flue gas purification solution storage tank enters a liquid drawing pool 10 through a pump 9 for standby. Mine water enters a coagulation tank 1, lime-sodium carbonate is added, then the mine water enters a filter 3 through a pump 2, the filter 3 is a tubular microfiltration system, and substances which are easy to scale, such as calcium, magnesium, silicon and the like in wastewater are removed and then the mine water enters a raw water tank 4 as raw water. Raw water in the raw water pool 4 enters the feed side of the forward osmosis membrane component 6 through the pump 5 to circularly flow; meanwhile, the draw solution in the draw solution tank 10 enters the draw solution side of the forward osmosis module 6 through the draw solution pump 11. Under the driving of osmotic pressure difference, the concentrated water discharged from the recycling system enters the side of the forward osmosis liquid drawing through the forward osmosis membrane component 6, and is concentrated while the triethanolamine concentrated solution is diluted. When the TDS of the concentrated water after forward osmosis concentration is 120000mg/L, the concentrated water is discharged through a valve 7 and then is sent to a rear-end evaporative crystallization unit. When the concentration of the diluted triethanolamine is 20%, the diluted triethanolamine is discharged through a valve 13 and then sent to a wet decarburization device to be used as absorption liquid.
The above is only the feasible embodiment of the utility model, not therefore the limit the patent scope of the utility model, all the events utilize the equivalent change of content place in the specification and the attached drawings all contain the protection scope of the utility model.
Claims (4)
1. The saline wastewater treatment system coupled with the flue gas purification treatment is characterized by comprising a raw water tank (4) and a flue gas purification liquid storage tank (8), wherein the raw water tank (4) is connected to the feed liquid side of a forward osmosis membrane assembly (6) through a pipeline, the outlet of the flue gas purification liquid storage tank (8) is connected with a liquid drawing tank (10), the outlet of the liquid drawing tank (10) is connected to the liquid drawing inlet of the forward osmosis membrane assembly (6) through a pipeline, and a liquid drawing pump (11) is arranged on the pipeline; the drawing liquid outlet of the forward osmosis membrane assembly (6) is connected to a flue gas purification and absorption device;
the inlet of the raw water pool (4) is connected with a pretreatment system, the pretreatment system comprises a coagulation tank (1) and a filter (3), and the coagulation tank (1), the filter (3) and the raw water pool (4) are sequentially connected;
a draw solution outlet at the draw solution side of the forward osmosis membrane assembly (6) is connected with an inlet of a draw solution pool (10) through a pipeline, and a draw solution circulating valve (12) is arranged on the pipeline;
be provided with dense water valve (7) between the feed liquid side export of forward osmosis membrane subassembly (6) and former pond (4), dense water valve (7) are the three-way valve, and the entry of dense water valve (7) and the feed liquid side exit linkage of forward osmosis membrane subassembly (6), and the first export and the dense water treatment facilities entry linkage of dense water valve (7), the second export and the former pond (4) of dense water valve (7) are connected.
2. The system for treating the saline wastewater coupled with the flue gas purification treatment, according to claim 1, characterized in that a raw water pump (2) is arranged between the coagulation tank (1) and the filter (3).
3. The system for treating the saline wastewater coupled with the flue gas purification treatment as recited in claim 1, wherein the concentrated water treatment device is an evaporative crystallization device.
4. The system for treating the salt-containing wastewater coupled with the flue gas purification treatment of claim 1, wherein the flue gas purification and absorption device is a wet desulfurization device, a wet denitrification device and/or a wet decarburization device.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110407369A (en) * | 2019-08-28 | 2019-11-05 | 陕西煤业化工技术研究院有限责任公司 | A kind of the brine waste processing system and processing method of coupling gas cleaning processing |
| CN114699893A (en) * | 2022-02-28 | 2022-07-05 | 华电水务工程有限公司 | Resource utilization method for high sulfate radical nanofiltration concentrated water |
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2019
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110407369A (en) * | 2019-08-28 | 2019-11-05 | 陕西煤业化工技术研究院有限责任公司 | A kind of the brine waste processing system and processing method of coupling gas cleaning processing |
| CN114699893A (en) * | 2022-02-28 | 2022-07-05 | 华电水务工程有限公司 | Resource utilization method for high sulfate radical nanofiltration concentrated water |
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