CN212954702U - Zero discharging equipment of power plant's high salt waste water - Google Patents
Zero discharging equipment of power plant's high salt waste water Download PDFInfo
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- CN212954702U CN212954702U CN202021152452.9U CN202021152452U CN212954702U CN 212954702 U CN212954702 U CN 212954702U CN 202021152452 U CN202021152452 U CN 202021152452U CN 212954702 U CN212954702 U CN 212954702U
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Abstract
The utility model relates to a high salt waste water zero release device of power plant, the device includes: the device comprises a high-density tank, a V-shaped filter tank, a clean water tank, an ultrafiltration device, a nanofiltration device, a reverse osmosis membrane concentration device, a flue gas waste heat evaporation crystallization device and a desulfurization tower. The utility model discloses can reduce power plant's high salt waste water zero release medicament use amount and solid waste water zero release waste production volume, it is short to possess the process flow, and the maintenance cost is low, and has realized the resourceization of soluble salt in the waste water, utilizes the flue gas waste heat to carry out the evaporative crystallization to the high salt water simultaneously, has reduced the running cost of power plant's high salt waste water zero release by a wide margin.
Description
Technical Field
The utility model relates to a high salt waste water zero release device of power plant belongs to coal fired power plant high salt waste water treatment field.
Background
The high-salinity wastewater of the coal-fired power plant in China is mainly reverse osmosis RO membrane strong brine of the power plant, circulating water sewage, resin regeneration wastewater, desulfurization wastewater and the like, wherein the water quantity of the reverse osmosis RO membrane strong brine and the circulating water sewage is very large, the TDS is about 4000ppm, the TDS exceeds the environmental-friendly emission index, and the desalting treatment is needed.
The existing desalination treatment method of reverse osmosis RO membrane strong brine and circulating water sewage in China is mainly and cannot be utilized basically by using the gradient utilization of power plant wastewater, the technical route mainly comprises the technical routes of pretreatment, membrane concentration and decrement, strong brine entering a desulfurization tower and strong brine entering fly ash, the final high brine is in the form of desulfurization wastewater due to the mode, the problem of desulfurization wastewater is solved by a final centralized technical means of the power plant, the desulfurization wastewater is high in treatment investment, high in operation cost and generally undesirable in operation due to the very complex components of the desulfurization wastewater, the concentrated solution and crystallized salt generated by desulfurization wastewater treatment cannot be recycled, only the treatment method of entering fly ash can be adopted, but the fly ash soluble salt and chlorine root exceed the standard, and finally no hidden danger of proper treatment and removal is formed, practices prove that the mode, the problem of zero discharge of the waste water of the power plant cannot be fundamentally solved, and the problem of the high-salinity waste water of the power plant cannot be fundamentally solved by adopting a solution of 'quality-based distribution'.
SUMMERY OF THE UTILITY MODEL
To the technical problem, the utility model provides a high salt waste water zero release device of power plant.
The utility model provides an above-mentioned technical problem's technical scheme as follows: a high salt waste water zero release device of power plant includes: the device comprises a high-density tank, a V-shaped filter tank, a clean water tank, an ultrafiltration device, a nanofiltration device, a reverse osmosis membrane concentration device, a flue gas waste heat evaporation crystallization device and a desulfurization tower;
the first inlet of the high-density tank is used for entering high-salinity wastewater, the second inlet of the high-density tank is a medicament adding port, the first outlet of the high-density tank is a precipitated sludge discharge port, the third inlet of the high-density tank is used for introducing backwashing water from the V-shaped filter tank, the ultrafiltration device, the nanofiltration device and the reverse osmosis membrane concentration device, and the second outlet of the high-density tank is a solution outlet and is connected to the first inlet of the V-shaped filter tank through a pipeline;
a first inlet of the V-shaped filter tank is a solution inlet, a second inlet of the V-shaped filter tank is a backwashing water inlet and is connected with a first outlet of the clean water tank, a first outlet of the V-shaped filter tank is a backwashing water outlet, and a second outlet of the V-shaped filter tank is a clean water outlet and is connected with an inlet of the clean water tank;
a first outlet of the clean water tank is a backwashing water outlet, a second outlet of the clean water tank is a solution outlet and is connected with a first inlet of the ultrafiltration device;
a second inlet of the ultrafiltration device is a backwashing water and medicament inlet, and a first outlet of the ultrafiltration device is a backwashing water outlet;
a first inlet of the nanofiltration device is connected with a second outlet of the ultrafiltration device, a second inlet of the nanofiltration device is a backwashing water inlet, a first outlet of the nanofiltration device is a backwashing water outlet, a second outlet of the nanofiltration device is a nanofiltration concentrated water outlet, and the second outlet of the nanofiltration device is connected with an inlet of the desulfurization tower through a pipeline;
the first inlet of the reverse osmosis membrane concentration device is connected with the third outlet of the nanofiltration device, the first outlet of the reverse osmosis membrane concentration device is a produced water outlet, the second inlet of the reverse osmosis membrane concentration device is a backwashing water inlet, the second outlet of the reverse osmosis membrane concentration device is a backwashing water outlet, the third inlet of the reverse osmosis membrane concentration device is a medicament adding port, the third outlet of the reverse osmosis membrane concentration device is a reverse osmosis concentrated brine outlet, and the third outlet of the reverse osmosis membrane concentration device is connected with the first inlet of the flue gas waste heat evaporation crystallization device through a pipeline;
the second inlet of the flue gas waste heat evaporation crystallization device is a high-temperature flue gas inlet, the first outlet of the flue gas waste heat evaporation crystallization device is a low-temperature flue gas outlet, the second outlet of the flue gas waste heat evaporation crystallization device is a condensate water outlet, and the third outlet of the flue gas waste heat evaporation crystallization device is a crystallized salt outlet.
The utility model has the advantages that:
1, the technical means of zero discharge of the reverse osmosis RO membrane strong brine and the circulating water sewage of the power plant with low operation cost is provided, and compared with the route of the prior art, the method can greatly reduce the usage amount of the medicament, the solid waste generated by wastewater treatment and the operation cost.
2. The technical process flow is short, the equipment structure is simple, the operation is easy, and the operation and maintenance cost is low.
3. The recycling of soluble salt in the reverse osmosis RO membrane strong brine and circulating water sewage of the power plant is realized, and the produced sodium chloride crystal salt can be applied to the industry.
4. The technical means of carrying out evaporative crystallization on the high-salinity wastewater after membrane concentration based on the mode of discharging flue gas waste heat outside a power plant is provided for the first time, so that the operation cost of evaporative crystallization is low.
5. The combination of the high-efficiency chelating agent and the nanofiltration device is provided, and the solubility of calcium sulfate in the wastewater is improved, so that the membrane is prevented from scaling and blocking in the nanofiltration concentration process, the aim of saving the cost of the softening agent is fulfilled, and the operation cost of pretreatment is greatly reduced.
Drawings
Fig. 1 is a block diagram of a structure of a method for zero discharge of high-salinity wastewater from a power plant according to an embodiment of the present invention;
fig. 2 is a block diagram of a flue gas waste heat evaporation crystallization device provided by the embodiment of the present invention.
Detailed Description
The principles and features of the present invention are described below in conjunction with the following drawings, the examples given are only intended to illustrate the present invention and are not intended to limit the scope of the present invention.
As shown in fig. 1, the whole set of device mainly comprises a high-density P, V type filter pool Q, a clean water pool R, an ultrafiltration device S, a nanofiltration device T, a reverse osmosis membrane concentration device U, a flue gas waste heat evaporation crystallization device W and a desulfurization tower V. The following are introduced separately:
1 high-Density pool P
High-salt wastewater enters the high-density pool P from the port 1, the agent adding port is the port 3, and the precipitated sludge discharging port is the port 2. The 4 ports are filled with flushing sewage from the V-shaped filter tank Q, the ultrafiltration device S, the nanofiltration device T and the reverse osmosis membrane concentration device U. The 5 ports are clean water outlets and are connected to the 6 ports of the V-shaped filter chamber Q through pipelines.
The reverse osmosis RO membrane strong brine of power plant, circulating water blowdown water, at first get into high density pond P through the feed liquor pump, high density pond P will coagulate, flocculate, deposit and sludge concentration function and assemble in an organic whole. Is divided into a mixing zone, a flocculation zone, a sedimentation zone and a pH adjusting zone. Coagulant is added into the mixing zone and is rapidly stirred, and the medicament and raw water are fully and uniformly mixed to form small floc. The pre-coagulated raw water flows to the bottom of a circular guide shell in the reaction tank, the raw water, the return sludge and the coagulant aid are uniformly mixed from bottom to top by a stirring paddle in the guide shell, the extremely high sludge concentration improves the flocculation effect, and the sludge enters a settling zone for rapid sedimentation and concentration after a larger flocculating constituent is formed. The inclined pipe is arranged in the sedimentation area, the residual alum blossom is retained on the inclined pipe, the residual alum blossom is combined into large alum blossom and then falls into the bottom of the pool, the effluent quality is ensured, and the effluent enters the next-stage treatment device after the pH value is adjusted. Part of the concentrated sludge is sent to the inlet of the reaction tank by a sludge circulating pump in the concentration area, and the other part of the concentrated sludge is used as residual sludge to be discharged to sludge dewatering or to be treated.
The effluent turbidity of the high-density pool P is less than 10NTU, and the COD removal rate in the wastewater is about 20 percent.
The high-density tank P is added with one or more mixed agents of inorganic polymeric flocculant (PAC polyaluminium chloride, PAFC polyaluminium ferric chloride, PFS polyferric sulfate) and organic polymeric flocculant PAM (polyacrylamide).
The sedimentation assisting magnetic particles and the magnetic particles are added into the reaction area of the high-density tank and are made of ferroferric oxide or similar materials, the sedimentation assisting magnetic particles realize rapid sedimentation through the magnetic bridging and framework effects of the magnetic particles, the sedimentation time is shortened by 40%, the clarification effect is improved, the volume of the high-density tank P is saved, and the equipment investment cost is reduced.
The high-density tank P only removes suspended matters in the wastewater, thereby saving the cost of softening agents.
2. V-shaped filter Q
The V-shaped filter Q is a form of filter. A V-shaped filter Q has 6 ports as a solution inlet, 8 ports as a backwashing water inlet, 7 ports as a backwashing sewage outlet and 9 ports as a clean water outlet, and is connected with a clean water tank R port 10.
After the water to be filtered passes through the adjustable weir plate, the water inlet gate and the square hole from the water inlet main channel, the water enters the V-shaped groove submerged by the water to be filtered through the side hole, and then enters the filter tank through the water distribution hole and the V-shaped groove weir which are uniform at the bottom of the tank. The filtered water flows into the bottom through the long-handle filter head, then flows into the gas water distribution pipe channel through the square hole, and then flows into the intermediate water pool through the water seal well, the water outlet weir and the clear water channel in the pipe gallery. The homogeneous filtering material is selected as the filtering material, so that the filtering material has higher filtering layer dirt intercepting capability, is relatively convenient to operate, manage and maintain, and can ensure the quality of the outlet water. The backwashing mode is matched with surface sweeping and air auxiliary scrubbing, and the V-shaped filter tank is mainly characterized in that:
(1) constant water level and constant speed filtration. The water producing valve of the filter tank is interlocked with the liquid level meter in the filter tank, and the opening degree is continuously adjusted along with the water level change, so that the water level in the filter tank is kept unchanged in the whole filtering period, and the negative pressure does not occur in the filter layer. When a certain filter is washed, part of water to be filtered continuously enters the lattice filter to be used as surface sweeping washing water, so that the water inlet load of other lattice filters is reduced;
(2) the homogeneous quartz sand filter material is adopted, the thickness of a filter layer is thicker than that of a common quick filter, and the pollutant interception capacity is also larger than that of the common quick filter, so the filter speed is higher, the filter period is long, and the water outlet effect is good;
(3) the V-shaped water inlet groove (which is also used as a surface sweeping water distribution groove during flushing) and the water discharge groove are arranged along the length direction of the tank, so that uniform water distribution is facilitated when the area of a single tank is large.
(4) The flushing adopts air-water combined backwashing and surface sweeping, so that the flushing effect is improved, and the flushing water is saved.
(5) When the sand filter is washed, the filter layer keeps a micro-expansion state, and the sand leakage phenomenon can be effectively avoided.
3. Clean water tank R
The purified clear water in the buffer tank flows out from the 12 ports and enters the ultrafiltration device S from the 13 ports.
4. Ultrafiltration device S
The 14 ports of the ultrafiltration device S are back washing water and medicament inlets, and the 15 ports are washing waste water discharge ports.
Consists of an ultrafiltration host machine, a backwashing system, a dosing system, a chemical cleaning system and the like. After the pretreated effluent is subjected to ultrafiltration treatment, most of turbidity and chromaticity in the influent can be effectively removed, and COD (chemical oxygen demand) substances can also be partially removed, so that the running stability of a subsequent reverse osmosis system is ensured. The ultrafiltration device S has the functions of intercepting tiny particles, reducing suspended matters, bacteria and turbidity, partially removing organic pollutants and achieving the purpose of improving and stabilizing water quality.
The ultrafiltration adopts an external pressure type hollow fiber ultrafiltration membrane, and has good pollution resistance and backwashing and cleaning recovery capabilities. In order to ensure that the system can operate safely and stably for a long time and avoid the membrane module from bearing higher operation load, the water flux of the membrane module is designed to be not more than 50L/(m2. h).
Suspended matters, colloid, bacteria, macromolecular organic matters and the like trapped by the ultrafiltration device are accumulated on the surface of the membrane, and the existence of the pollutants can influence the normal filtration of the system. In order to ensure the stable operation of the system and keep good dirt removing capability, a back washing device is equipped to periodically back wash the ultrafiltration device. In order to carry out backwashing more thoroughly, an air-water combined backwashing mode is adopted, backwashing water source adopts ultrafiltration to produce water, and compressed air required by backwashing comes from a process compressed air storage tank.
The matched sodium hypochlorite dosing device 1 set (comprising a sodium hypochlorite storage tank, a sodium hypochlorite discharging pump, a sodium hypochlorite dosing pump and the like), an acid dosing device and an alkali dosing device.
3) Chemical reinforced backwashing device
In order to recover the filtration flux of the ultrafiltration membrane and prolong the chemical cleaning period, chemical agents can be added into backwashing water irregularly during backwashing of the ultrafiltration membrane, and the ultrafiltration membrane is respectively subjected to acid cleaning and alkali cleaning. Hydrochloric acid/citric acid is adopted for acid washing, and NaOH + NaClO is adopted for alkali washing.
4) Ultrafiltration chemical cleaning device
After the ultrafiltration device is operated for a long time, certain dirt which is difficult to remove by normal backwashing or chemical reinforced backwashing can be accumulated, such as reproduction of organic matters and microorganisms, and the flux of the ultrafiltration membrane is reduced, and then the device needs to be subjected to restorative chemical cleaning to restore the performance of the ultrafiltration membrane.
5. Nanofiltration device T
And a 17 port of the nanofiltration device T is connected with a 16 port of the ultrafiltration device S to be used as a water inlet, a 21 port is a backwashing inlet, a 19 port is a backwashing waste liquid outlet, nanofiltration concentrated water is discharged from a 20 port and is connected with a 22 port through a pipeline, the nanofiltration concentrated water enters a desulfurization system to be used as make-up water of the desulfurization system, the nanofiltration concentrated water amount is lower than about 30 percent of the total water inflow amount, and the nanofiltration water yield is about 70 percent. The nanofiltration produced water flows out of the 24 ports and enters the 25 ports of the reverse osmosis membrane concentration device U.
Nanofiltration membranes can trap nano-sized (0.001 micron) substances. The operating interval of the nanofiltration membrane is between ultrafiltration and reverse osmosis, the molecular weight of the intercepted organic matter is about 200-800MW, the capacity of intercepting dissolved salts is 20% -98%, the removal rate of soluble monovalent ions is lower than that of high valence ions, the nanofiltration membrane is generally used for removing the organic matter and pigment in surface water, the hardness and radium in underground water, and partially removing the dissolved salts, and the extraction and concentration of useful substances in food and medicine production. The operating pressure of the nanofiltration membrane is generally 3.5-30 bar.
The interception rate of the ions with more than two valences by adopting nanofiltration is 98 percent. The nanofiltration membrane adopts an anti-pollution membrane, wherein the COD tolerance reaches more than 300 ppm.
The nanofiltration membrane can adopt a roll type nanofiltration membrane or a flat plate type nanofiltration membrane.
The nano-filtration water inlet front end is provided with a dosing device, the added chelating agent is fed from 18 openings, the chelating agent is continuously added, the chelating agent is combined with calcium sulfate to generate a composite soluble calcium salt, the composite soluble calcium salt is dissolved in a solution, the precipitation of the calcium sulfate is avoided, the effect of preventing fouling and blocking the membrane is achieved, the chelating agent improves the solubility of the calcium sulfate by more than 5 times, and the chelating agent needs to be continuously added.
The addition amount of the chelating agent is less than 30ppm
By adding the chelating agent, the hardness of the high-salinity wastewater entering the nanofiltration is not required to be reduced, the calcium and magnesium are removed, and the cost of the agent is reduced by more than 70%.
6. Reverse osmosis membrane concentration device U
25 water inlets and 27 water outlets of the reverse osmosis membrane concentration device U are a water outlet, 28 backwash liquid inlets, 26 backwash liquid outer discharge ports, 29 medicament adding ports, and 30 reverse osmosis concentrated brine is discharged from 31 ports of the flue gas waste heat evaporation crystallization device W through a pipeline.
The reverse osmosis membrane adopts an anti-pollution reverse osmosis membrane, the reverse osmosis RO membrane can be designed into two stages, the first stage adopts a low-pressure common reverse osmosis membrane, the rated water yield of the reverse osmosis membrane reaches 80%, the second stage can adopt a medium-pressure reverse osmosis RO membrane, the water yield is not lower than 70%, and the second stage reverse osmosis membrane adopts a seawater desalination membrane.
The reverse osmosis membrane is mature and reliable in technology and comprises a pressure pump, a reverse osmosis membrane group, an online instrument, a prying seat, a valve group, an online instrument and the like.
After long-term operation, the RO membrane can accumulate certain dirt which is difficult to wash, such as organic matters, inorganic salt scaling and the like, and the flux of the performance of the RO membrane is reduced. Such foulants must be removed by cleaning with chemicals to restore the performance of the reverse osmosis membrane. The reverse osmosis membrane needs to be chemically cleaned once when running for 1-3 months according to the water quality condition so as to ensure the water permeability of the membrane. And respectively carrying out acid washing and alkali washing on the reverse osmosis membrane. Hydrochloric acid/citric acid is used for acid washing, and sodium hydroxide or a specific cleaning agent is used for alkali washing.
7. Flue gas waste heat evaporation crystallization device W
As shown in fig. 2, the device mainly comprises a flue gas heat exchanger a, a first-effect evaporator B, a second-effect crystallizer C, a closed water cooling tower D, a circulating pump E, a buffer water tank F, a circulating pump G, a discharge pump H, a heat exchanger I, a flash tank K, a fan L, a feed pump M, a vacuum device N and a noncondensable gas heat exchanger O.
The flue gas temperature is higher than 110 ℃, the flue gas after heat exchange is discharged from the outlet 35 of the flue gas waste heat evaporation crystallization device W, the temperature is not lower than 110 ℃, condensed water is discharged from the outlet 32, the condensed water is a condensed water outlet of the heat exchanger I, and the outlet 33 of the heat exchanger I is a crystallized salt outlet of the double-effect crystallizer C.
The 31 port of the flue gas waste heat evaporation crystallization device W is an inlet of a feeding pump M, the high-temperature flue gas inlet 34 is an inlet of a flue gas heat exchanger A, and the low-temperature flue gas outlet 35 after heat exchange is an outlet of the flue gas heat exchanger A.
Reverse osmosis membrane enrichment facility U strong brine is connected by 30 mouths and 31 mouths, be connected with flue gas waste heat evaporation crystallization device W's charge pump M, get into noncondensable gas heat exchanger O through charge pump M, after the heat transfer, high salt water gets into closed cooling tower D, the make-up water of closed cooling tower D is regarded as to high salt water, closed cooling tower D is connected with fan L, air inlet and the high salt solution that sprays in closed cooling tower D tower and the heat transfer of tube heat exchanger wall in the tower, steam cooling liquefaction becomes the comdenstion water in the heat exchanger pipe, wind absorbs moisture in the salt water, air saturated discharges the atmosphere, the evaporation of moisture in the salt water has been realized.
The closed water cooling tower D forms the circulation of the high-salinity water solution in the closed water cooling tower D and the circulating pump E through a connected pipeline. A high-salinity concentrated water outlet of a closed water cooling tower D passes through a discharge pump H and enters a heat exchanger I through a pipeline, heat exchange is carried out in the heat exchanger I, the heat exchanger I adopts a plate type or tube type heat exchanger, condensed water of a double-effect crystallizer C and condensed water of the outer row of a first-effect evaporator B are subjected to heat exchange, the cooled condensed water is discharged from the outer row port of the heat exchanger I, the heated high-salinity water enters a buffer water tank F through a pipeline, the buffer water tank F is a heat preservation water tank, the buffer water tank F is connected with a circulating pump G, the circulating pump G is connected with a flue gas heat exchanger A, the heated high-salinity water enters a flash tank K through heat exchange, and flash steam of the flash tank K enters the heat exchanger with the first-effect. High salt water in the flash tank K is connected with the buffer water tank F through a connected pipeline, the buffer water tank F, the circulating pump G and the flue gas heat exchanger A are formed, the closed circulation of the flash tank K is realized, and the high-efficiency heat exchange of flue gas and high-salt wastewater is realized.
The high-salinity wastewater outlet end solution of the flue gas heat exchanger A enters a first-effect evaporator B, secondary steam of the first-effect evaporator B is connected with a second-effect crystallizer C through a steam pipeline, a steam pipeline at the tail end of the second-effect crystallizer C is connected with an internal coil heat exchanger of a closed water cooling tower D, and heat exchange, cooling and condensation are carried out in the tower of the closed water cooling tower D.
Vacuum pump unit N plays the effect of maintaining the entire system vacuum, maintains the negative pressure state of system, and one-effect evaporator B, two-effect crystallizer C, closed cooling tower D are connected with vacuum pump unit N through the pipeline respectively, and vacuum pump unit N's noncondensable gas export is connected with noncondensable gas heat exchanger O.
The flue gas heat exchanger A adopts a low-temperature tube type economizer or a low-temperature heat pipe type heat exchanger, the contact surface of the flue gas heat exchanger A and flue gas adopts a fin tube type, the pipe wall is coated with a corrosion-resistant, wear-resistant and high-efficiency heat transfer composite ceramic coating, the ceramic coating is composed of inorganic silicon oxide, silicon carbide and a high-temperature binder, the wall surface is firmly bonded, the tube side of the flue gas heat exchanger A is flowing high-salt wastewater, the heating section of the flue gas heat exchanger A is in contact with the flue gas, and flowing high-salt water is in the tube side.
The first-effect evaporator B can adopt a falling-film evaporator, a forced circulation evaporator, a climbing-film evaporator and the like.
The forced circulation crystallizer of the double-effect crystallizer C, the described first-effect evaporator B and the forced circulation crystallizer of the double-effect crystallizer C all adopt a three-phase flow fluidized bed anti-scaling technology;
the working principle of the water cooling tower is as follows: the air blown in and the water sprinkled from the air form convection to remove the heat source, and part of the water is evaporated in the convection to take away the corresponding latent heat of evaporation, thereby reducing the temperature of the water. The cooling tower consists of a tower body, internal fillers, a top demister and a heat exchange coil, wherein the heat exchange coil is made of corrosion-resistant 316L and 2205 dual-phase steel or titanium.
The cooling tower is an atmospheric coagulation type cooling tower. Closed cooling tower D realizes becoming water with two-effect crystallizer C export steam cooling, and the latent heat of steam is taken away by the wind through closed cooling tower D, evaporates partial high salt waste water through the convection current mode simultaneously, realizes the concentrated decrement to high salt waste water.
The circulating pump E overflowing part is made of corrosion-resistant metal materials such as corrosion-resistant 316L and 2205 dual-phase steel, the buffer water tank F is a heat-preservation corrosion-resistant water tank, and the circulating pump G and the circulating pump E overflowing part are made of corrosion-resistant metal materials such as corrosion-resistant 316L and 2205 dual-phase steel; the discharge pump H overflowing piece is made of corrosion-resistant metal materials such as corrosion-resistant 316L and 2205 dual-phase steel; heat exchanger I adopts plate-type or shell and tube heat exchanger, realizes comdenstion water and high salt solution heat transfer, and high salt solution heaies up, and the comdenstion water is discharged after cooling to play the thermal effect of recovery comdenstion water:
after the high-salinity water heated by the flue gas enters a flash tank with lower pressure, the saturated water is changed into a part of saturated vapor and saturated water under the container pressure due to the sudden reduction of the pressure, the separation of the vapor and the water on the liquid level in the flash tank is realized, and the vapor generated after the separation enters a one-effect evaporator.
The flash tank adopts a circular cylinder made of corrosion-resistant metal materials such as corrosion-resistant 316L and 2205 dual-phase steel, and water is vaporized into steam under the negative pressure state.
The fan L adopts a common booster fan. The fan blows air of a certain flow into the closed water cooling tower D through pressurization, and contact heat exchange of the air in the water cooling tower D and the coil heat exchange pipe wall of sprayed high-salt water and low-temperature steam is achieved.
The overflow piece of the feed pump M is made of corrosion-resistant metal materials such as corrosion-resistant 316L and 2205 dual-phase steel, and the feed pump M conveys the high-salinity wastewater into the system.
The vacuum device N maintains the vacuum degree of the system and adopts a Roots water circulation vacuum unit or a steam jet type vacuum pump.
The non-condensable gas heat exchanger O adopts a plate type or tube type heat exchanger.
8. Desulfurizing tower I
The desulfurizing tower I adopts wet desulfurization and is widely applied environment-friendly equipment. And (3) enabling a 22-port of the desulfurizing tower I to enter nanofiltration concentrated water of a nanofiltration device T to serve as make-up water of the desulfurizing tower, and discharging desulfurized concentrated wastewater from a 23-port of the desulfurizing tower I.
Proved by experiments, the method provided by the embodiment of the utility model has the following beneficial effects:
1, the technical means for zero discharge of the reverse osmosis RO membrane strong brine and the circulating water sewage of the power plant with low operation cost is provided, compared with the prior art route, the usage amount of the medicament is reduced by more than 70%, the solid waste generated by wastewater treatment is reduced by more than 60%, the operation cost is reduced by more than 40%, and the wastewater recycling efficiency is 100%.
2. The technical process flow is short, the equipment structure is simple, the operation is easy, and the operation and maintenance cost is low.
3. The recycling of soluble salt in the reverse osmosis RO membrane strong brine and circulating water sewage of the power plant is realized, the purity of the produced sodium chloride crystal salt reaches more than 99 percent, and the industrial-grade use standard is met.
4. The technical means of carrying out evaporative crystallization on the high-salinity wastewater after membrane concentration based on the mode of discharging flue gas waste heat outside a power plant is provided for the first time, so that the operation cost of evaporative crystallization is low.
5. The combination of the high-efficiency chelating agent and the nanofiltration device is provided, the solubility of calcium sulfate in the wastewater is improved through the chelating agent, and the membrane is ensured not to be scaled and blocked in the nanofiltration concentration process, so that the aim of saving the expense of the softening agent is fulfilled, and the operation cost of pretreatment is greatly reduced.
The above description is only for the preferred embodiment of the present invention, and is not intended to limit the present invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included within the protection scope of the present invention.
Claims (6)
1. The utility model provides a high salt waste water zero release device of power plant which characterized in that includes: the device comprises a high-density tank, a V-shaped filter tank, a clean water tank, an ultrafiltration device, a nanofiltration device, a reverse osmosis membrane concentration device, a flue gas waste heat evaporation crystallization device and a desulfurization tower;
the first inlet of the high-density tank is used for entering high-salinity wastewater, the second inlet of the high-density tank is a medicament adding port, the first outlet of the high-density tank is a precipitated sludge discharge port, the third inlet of the high-density tank is used for introducing backwashing water from the V-shaped filter tank, the ultrafiltration device, the nanofiltration device and the reverse osmosis membrane concentration device, and the second outlet of the high-density tank is a solution outlet and is connected to the first inlet of the V-shaped filter tank through a pipeline;
a first inlet of the V-shaped filter tank is a solution inlet, a second inlet of the V-shaped filter tank is a backwashing water inlet and is connected with a first outlet of the clean water tank, a first outlet of the V-shaped filter tank is a backwashing water outlet, and a second outlet of the V-shaped filter tank is a clean water outlet and is connected with an inlet of the clean water tank;
a first outlet of the clean water tank is a backwashing water outlet, a second outlet of the clean water tank is a solution outlet and is connected with a first inlet of the ultrafiltration device;
a second inlet of the ultrafiltration device is a backwashing water and medicament inlet, and a first outlet of the ultrafiltration device is a backwashing water outlet;
a first inlet of the nanofiltration device is connected with a second outlet of the ultrafiltration device, a second inlet of the nanofiltration device is a backwashing water inlet, a first outlet of the nanofiltration device is a backwashing water outlet, a second outlet of the nanofiltration device is a nanofiltration concentrated water outlet, and the second outlet of the nanofiltration device is connected with an inlet of the desulfurization tower through a pipeline;
the first inlet of the reverse osmosis membrane concentration device is connected with the third outlet of the nanofiltration device, the first outlet of the reverse osmosis membrane concentration device is a water production outlet, the second inlet of the reverse osmosis membrane concentration device is a backwashing water inlet, the second outlet of the reverse osmosis membrane concentration device is a backwashing water outlet, the third inlet of the reverse osmosis membrane concentration device is a medicament adding port, the third outlet of the reverse osmosis membrane concentration device is a reverse osmosis concentrated brine outlet, and the reverse osmosis concentrated brine outlet is connected with the first inlet of the flue gas waste heat evaporation crystallization device through a pipeline;
the second inlet of the flue gas waste heat evaporation crystallization device is a high-temperature flue gas inlet, the first outlet of the flue gas waste heat evaporation crystallization device is a low-temperature flue gas outlet, the second outlet of the flue gas waste heat evaporation crystallization device is a condensate water outlet, and the third outlet of the flue gas waste heat evaporation crystallization device is a crystallized salt outlet.
2. The power plant high salinity waste water zero discharging device of claim 1, characterized in that, the flue gas waste heat evaporation crystallization device includes: the system comprises a flue gas heat exchanger, a first-effect evaporator, a second-effect crystallizer, a closed water cooling tower, a first circulating pump, a buffer water tank, a second circulating pump, a discharge pump, a heat exchanger, a flash tank, a fan, a feed pump, a vacuum device and a non-condensable gas heat exchanger;
an inlet of the feed pump is used as a first inlet of the flue gas waste heat evaporation and crystallization device, an outlet of the feed pump is connected with a first inlet of the non-condensable gas heat exchanger, and an outlet of the non-condensable gas heat exchanger is a strong brine outlet and is connected with a first inlet of the closed water cooling tower;
the second inlet of the closed water cooling tower is connected with the outlet of the fan, the first outlet of the closed water cooling tower is a high-salt water outlet, the first outlet of the closed water cooling tower is connected with the third inlet of the closed water cooling tower through the first circulating pump, high-salt water circulation is achieved, the second outlet of the closed water cooling tower is a high-salt water outlet, the second outlet of the closed water cooling tower is connected with the first inlet of the heat exchanger through the discharge pump, and the fourth inlet of the closed water cooling tower is connected with the first outlet of the secondary crystallizer;
the second inlet and the third inlet of the heat exchanger are condensed water inlets and are respectively connected with the first outlet of the first-effect evaporator and the second outlet of the second-effect crystallizer, the first outlet of the heat exchanger is a condensed water outlet, the second outlet of the heat exchanger is a high-salinity water outlet subjected to heat exchange and temperature rise and is connected with the inlet of the buffer water tank, and the second outlet of the heat exchanger is used as the second outlet of the flue gas waste heat evaporation and crystallization device;
the outlet of the buffer water tank is connected with the first inlet of the flue gas heat exchanger through a second circulating pump, the first outlet of the flue gas heat exchanger is connected with the inlet of the flash tank, the first outlet of the flash tank is connected with the second inlet of the buffer water tank, the second inlet of the flue gas heat exchanger is used as the second inlet of the flue gas waste heat evaporation and crystallization device, the second outlet of the flue gas heat exchanger is used as the first outlet of the flue gas waste heat evaporation crystallization device, a third outlet of the flue gas heat exchanger is connected with a first inlet of the first-effect evaporator, a second outlet of the flash tank is connected with a second inlet of the first-effect evaporator, a second outlet and a third outlet of the first-effect evaporator are respectively connected with a first inlet and a second inlet of the second-effect crystallizer, a third outlet of the two-effect crystallizer is used as a third outlet of the flue gas waste heat evaporation crystallization device;
and a fourth outlet of the first-effect evaporator, a fourth outlet of the second-effect crystallizer and a third outlet of the closed water cooling tower are connected with an inlet of the vacuum device, and an outlet of the vacuum device is connected with a second inlet of the non-condensable gas heat exchanger.
3. The power plant high-salinity wastewater zero-discharge device according to claim 1, characterized in that the ultrafiltration device is an external pressure type hollow fiber ultrafiltration membrane.
4. The power plant high-salinity wastewater zero-discharge device according to claim 1, wherein the nanofiltration membrane of the nanofiltration device is a rolled nanofiltration membrane or a flat nanofiltration membrane.
5. The power plant high salinity wastewater zero discharge apparatus according to claim 2, characterized in that, the vacuum device adopts roots water circulation vacuum unit or steam jet type vacuum pump.
6. The power plant high-salinity wastewater zero-discharge device according to claim 2, characterized in that the non-condensable gas heat exchanger is a plate-type or tube-type heat exchanger.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113023998A (en) * | 2021-04-14 | 2021-06-25 | 吉林省铸洁环保有限责任公司 | Desulfurization waste water zero release processing system based on bypass flue evaporation |
| CN116199370A (en) * | 2023-01-17 | 2023-06-02 | 济宁华源热电有限公司 | Hierarchical integrated processing system of thermal power plant, steam power plant's waste water |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113023998A (en) * | 2021-04-14 | 2021-06-25 | 吉林省铸洁环保有限责任公司 | Desulfurization waste water zero release processing system based on bypass flue evaporation |
| CN116199370A (en) * | 2023-01-17 | 2023-06-02 | 济宁华源热电有限公司 | Hierarchical integrated processing system of thermal power plant, steam power plant's waste water |
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