CN210237361U - High-salinity wastewater steady-state recycling device - Google Patents
High-salinity wastewater steady-state recycling device Download PDFInfo
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- CN210237361U CN210237361U CN201920654294.8U CN201920654294U CN210237361U CN 210237361 U CN210237361 U CN 210237361U CN 201920654294 U CN201920654294 U CN 201920654294U CN 210237361 U CN210237361 U CN 210237361U
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Abstract
The utility model provides a high salt waste water steady state resourceful device, includes preprocessing device, water resource recovery unit, liquid phase divides matter device, deep purification device and salinity recovery unit, connects through pipeline and liquid pump between each device. The utility model has the advantages that not only solved the processing problem of produced big amount of high salt waste water in the industrial production process, reached the zero release and retrieved the dual purpose of valuable salinity such as sodium sulfate, sodium chloride, sodium nitrate, realize resource cyclic utilization, have general adaptability to the high salt waste water that different salinities of different trades are constituteed moreover, the operation is stable, and the management of being convenient for has apparent economic benefits and social.
Description
Technical Field
The utility model relates to an industrial waste water retrieval and utilization and zero release equipment, in particular to high salt waste water steady state resourceful device.
Background
The 'reuse of reclaimed water' is an effective way for realizing the reclamation of industrial wastewater and saving industrial water, the 'zero discharge' of the industrial wastewater can reduce the diffusion of pollutants to the external environment and reduce the environmental burden, and the two play important roles in promoting and regulating water resource protection, water pollution treatment and economic sustainable development. The industrial wastewater output in China is large, the coverage is wide, the types are various, the treatment difficulty is large, and the cost is high. In coal chemical industry, petrifaction, steel, power plants, papermaking, printing and dyeing and other water consumers, zero discharge of waste water is undoubtedly the primary requirement of the water consumers due to the characteristics of large water discharge, multiple water discharge points, complex water discharge quality and the like. The sewage of the enterprises is basically divided into two types, one is high-pollution and low-salt production wastewater, and the wastewater mainly comes from the drainage of each production device. The other type is low-pollution and salt-containing wastewater which mainly comes from concentrated water of a desalted water station, circulating cooling sewage and the like. The traditional wastewater treatment process is to treat high-pollution and low-salt production wastewater by adopting a process mainly based on biochemical treatment, remove pollutants such as organic matters, ammonia nitrogen and the like in the wastewater, combine the wastewater with the low-pollution and salt-containing wastewater for recycling treatment, recycle water is recycled by adopting a process mainly based on a membrane method as circulating water for replenishing water, and realize industrial water saving, and meanwhile, the generated high-salt wastewater is finally subjected to zero emission.
However, the high-salinity wastewater generated in the above industries generally contains a large amount of valuable inorganic chemical raw materials such as sodium sulfate, sodium chloride, sodium nitrate and the like, and the conventional zero-emission process of the high-salinity wastewater usually converts the high-salinity wastewater into mixed salt, so that the high-salinity wastewater becomes dangerous waste, the treatment cost is very high and reaches 10000 yuan/ton in addition to 5000 plus materials, and heavy metals and organic pollutants doped in the mixed salt are easy to dissolve and seep out when meeting water, so that the potential hazard of secondary pollution exists.
Nowadays, a novel 'high-salinity wastewater recycling' process taking nanofiltration separation as a core unit is adopted by more and more zero-emission salt separation projects so as to recover valuable salts in high-salinity wastewater as much as possible. But due to the characteristic that the nanofiltration separation effect is easily impacted by water quality fluctuation, the salt recovery effect is not ideal, the recovery rate is low, and the salt product is unstable, so that the coping requirements of enterprises on increasingly strict environmental protection policies are difficult to meet.
Disclosure of Invention
The utility model aims at providing a high salt waste water steady state resourceful treatment equipment to the defect that exists among the prior art.
The utility model discloses a treatment facility includes preprocessing device, water resource recovery unit, liquid phase branch matter device, salinity recovery unit, connects through pipeline and liquid pump between each device, and its characterized in that preprocessing device is: the water outlet of the high-salinity wastewater regulating tank 101 is connected with the water inlet of the COD degradation device 102 through a pipeline and a regulating tank lift pump 109. The water outlet of the COD degradation device 102 is connected to the softening and desiliconizing device 103 through a pipeline and a softening and desiliconizing device water inlet pump 110. The water outlet of the softening and silicon-removing device 103 is connected to the intermediate water tank 104 through a pipeline and an intermediate water pump 111. The sludge outlet of the softening and desiliconizing device 103 is pumped to the sludge treatment device A105. The outlet of the intermediate water basin 104 is connected to the ion exchange unit 106 via a pipe and an ion exchange unit inlet pump 112. The water outlet of the ion exchange unit is connected to a pretreatment effluent pool 107 through a pipeline. The ion exchange device 106 is provided with a regenerant addition device 108. The regenerated liquid is periodically discharged to the high-salinity wastewater adjusting tank 101.
The water resource recovery device is as follows: the outlet of the pretreatment effluent pool 107 is connected with a cartridge filter A201 through a pipeline and a reverse osmosis device inlet pump 210. The outlet of the cartridge filter a201 is connected to the reverse osmosis unit 202 via a pipe and a reverse osmosis high-pressure pump 211. The reverse osmosis device 202 is connected with the outlet of the antisludging agent feeding device A203 through a pipeline. The cleaning inlet and outlet of the reverse osmosis device 202 are respectively connected with the outlet and inlet of the chemical cleaning device A204 through pipelines. The water production port of the reverse osmosis unit 202 is connected to a reuse water tank 208 via a pipeline. The concentrate inlet of the reverse osmosis unit 202 is connected to the super concentrator 205 via a pipe and a super concentrator feed pump 207. The water production port of the super concentrator 205 is piped to the reuse water tank 208. The concentrate inlet of the super concentrator 205 is connected to a concentrate tank 209 via a pipe. The cleaning port of the super concentrator 205 is connected to the outlet and inlet of the chemical cleaning device B206, respectively.
The liquid phase quality separation device comprises: the outlet of the concentrated water tank 209 is connected with a security filter B301 through a pipeline and a nanofiltration device water inlet pump 305. The outlet of the security filter B301 is connected with a nanofiltration device 302 through a pipeline and a nanofiltration high-pressure pump 306. The nanofiltration device 302 is connected with an outlet of the scale inhibitor feeding device B303 through a pipeline. The cleaning inlet and outlet of the nanofiltration device 302 are respectively connected with the outlet and inlet of the chemical cleaning device C304 through pipelines. The water producing port of the nanofiltration device 302 is connected to the brine tank 307 through a pipeline. The concentrate inlet of the nanofiltration device 302 is connected to a nitrate water tank 308 through a pipeline.
The salinity recovery unit is: the outlet of the brine tank 307 is connected to the # 1 crystallization device 401 via a pipe and a water inlet pump 410 of the # 1 crystallization device. An evaporation condensate outlet is connected to a condensate water pool 405 through a pipeline and a No. 1 condensate water pump 413. The mother liquor discharge port is connected with a mother liquor pool 406 through a pipeline and a # 1 mother liquor pump 415. The nitrate water tank 308 is connected to the No. 2 crystallizing device 402 through a pipeline and a water inlet pump 411 of the No. 2 crystallizing device. The mother liquor discharge port is connected with the intermediate water tank 409 through a pipeline and a 2# mother liquor pump 416. The intermediate salt separated by the No. 2 crystallizing device 402 is sent to the No. 3 crystallizing device hot melting tank 404 through a conveyer belt. The evaporation condensate collected in condensate tank 405 is used to redissolve the salt. The outlet of the hot melt tank 404 of the 3# crystallization device is connected with the 3# crystallization device 403 through a pipeline and a 3# crystallization device water inlet pump 412. An evaporation condensate outlet of the No. 3 crystallizing device 403 is connected to a condensate water tank 405 through a pipeline and a No. 3 condensate water pump 414. The mother liquor discharge port discharges into the mother liquor tank 406 through a pipe and a # 3 mother liquor pump 417. The outlet of the mother liquor tank 406 is connected with a mother liquor solidification device 407 through a pipeline and a mother liquor solidification device water inlet pump 418. The cleaning ports of the 1# crystallization device 401, the 2# crystallization device 402, the 3# crystallization device 403 and the mother liquor solidification device 407 are respectively connected with the outlet and the inlet of a chemical cleaning device D408.
The depth purification device is: the outlet of the intermediate salt recovery water tank 409 is connected to the deep purification device 501 through a pipeline and a deep purification device water inlet pump 503, the water outlet of the deep purification device 501 is connected to the concentrated water tank 209 through a pipeline and a purification mother liquid pump 504, and the sludge outlet of the deep purification device 501 is pumped to a sludge treatment device B502.
The COD degradation device 102 is a combination of advanced oxidation and biochemical treatment.
The softening and desiliconizing device 103 is a combined device of medicament reaction, high-efficiency clarification and immersed ultrafiltration.
The cation exchange resin of the ion exchange device 106 is a macroporous cation exchange resin suitable for adsorption of divalent cations.
The reverse osmosis membrane of the reverse osmosis device 202 is an anti-pollution type brackish water membrane and an anti-pollution type sea fresh membrane, the recovery rate of produced water is 60-90%, and the desalination rate is more than or equal to 97%.
The super concentration device 205 is a low-temperature evaporation concentration device, and the concentration multiple is 2-4.
The nanofiltration membrane of the nanofiltration device 302 is a high-precision mono-divalent separation nanofiltration membrane component, the yield of produced water is more than or equal to 40%, and the retention rate of divalent salt is more than or equal to 95%.
The No. 1 crystallizing device 401 and the No. 3 crystallizing device 403 are crystallizing complete equipment which is a steam-driven multiple-effect evaporative crystallizer (MEE), a steam mechanical recompression evaporative crystallizer (MVR), a steam power recompression evaporative crystallizer (TVR) or a cooling crystallizer (DTB) with a guide flow cylinder.
The 2# crystallization device 402 is a crystallization complete equipment which is a cooling crystallizer (DTB) with a guide shell.
The mother liquid solidifying device 407 is a spray drying device or a rake drying device.
The mother liquor solidification device 407 can be omitted from use in the condition of disposing in a mother liquor discharge set.
After the nanofiltration device 302 and the 2# crystallization device 402 are exchanged, the outlet of the concentrated water tank 209 is connected with the inlet of the 2# crystallization device 402 through a pipeline and a water inlet pump 411 of the 2# crystallization device.
After the nanofiltration device 302 and the 2# crystallization device 402 are exchanged, the outlet of the salt recovery intermediate water tank 409 is connected with a security filter B301 through a pipeline and a nanofiltration device water inlet pump 305, and the outlet of the security filter B301 is connected with the nanofiltration device 302 through a pipeline and a nanofiltration high-pressure pump 306.
After the nanofiltration device 302 and the 2# crystallization device 402 are exchanged, the outlet of the saltpeter water tank 308 is connected with the deep purification device 501 through a pipeline and a deep purification device water inlet pump 503, and the outlet of the deep purification device 501 is connected with the inlet of the concentrated water tank 209 through a pipeline and a purified mother liquor water outlet pump 504.
The utility model has the advantages that not only solved the processing problem of produced big amount of high salt waste water in the industrial production process, reached the zero release and retrieved the dual purpose of valuable salinity such as sodium sulfate, sodium chloride, sodium nitrate, realize resource cyclic utilization, have general adaptability to the high salt waste water that different salinities of different trades are constituteed moreover, the operation is stable, and the management of being convenient for has apparent economic benefits and social.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a block diagram of the process of the present invention.
In the figure: 101 high-salinity wastewater regulating tank, 102COD degradation device, 103 softening and desiliconizing device, 104 intermediate water tank, 105 sludge treatment device A, 106 ion exchange device, 107 pretreatment water outlet tank, 108 regenerant adding device, 109 regulating tank lift pump, 110 softening and desiliconizing device water inlet pump, 111 intermediate water pump, 112 ion exchange device water inlet pump, 201 cartridge filter A, 202 reverse osmosis device, 203 antisludging agent adding device A, 204 chemical cleaning device A, 205 super concentrating device, 206 chemical cleaning device B, 207 super concentrating device water inlet pump, 208 reuse water tank, 209 concentrated water tank, 210 reverse osmosis device water inlet pump, 211 reverse osmosis high-pressure pump, 301 cartridge filter B, 302 nanofiltration device, 303 antisludging agent adding device B, 304 chemical cleaning device C, 305 nanofiltration device water inlet pump, 306 nanofiltration high-pressure pump, 307 brine tank, 308 nitrate water tank, 4011 # crystallization device, 4022 # crystallizing device, 4033 # crystallizing device, 4043 # crystallizing device hot-melt pool, 405 condensed water pool, 406 # mother liquid pool, 407 # mother liquid solidifying device, 408 chemical cleaning device D, 409 salt recovery intermediate water pool, 4101 # crystallizing device water inlet pump, 4112 # crystallizing device water inlet pump, 4123 # crystallizing device water inlet pump, 4131 # condensed water pump, 4143 # condensed water pump, 4151 # mother liquid pump, 4162# mother liquid pump, 4173 # mother liquid pump, 418 mother liquid solidifying device water inlet pump, 501 deep purification device, 502 sludge processing device B, 503 deep purification device water inlet pump, 504 purification mother liquid outlet pump.
Detailed Description
Example one
The embodiments of the present invention will be further explained with reference to the accompanying drawings:
the device comprises a pretreatment device, a water resource recovery device, a liquid phase quality separation device, a salinity recovery device and a deep purification device, wherein all the devices are connected through a pipeline and a liquid pump. Taking the strong brine wastewater to be treated of a typical coal chemical industry zero discharge device as an example, the water inlet amount is 60m3The salt content is 1.0 percent, wherein the main salts are sodium sulfate and sodium chloride, sulfate radical is 1110mg/L, chloride radical is 4980mg/L, COD is 180mg/L, the total hardness is 1000mg/L, the total alkalinity is 2000mg/L, and the soluble silicon content is 120mg/L, after the treatment of the high-salinity wastewater steady state recycling device, the yield of the industrial salt is more than 95 percent, and the yield of the reuse water is more than 98 percent.
The treatment facility of this embodiment includes preprocessing device, water resource recovery unit, liquid phase branch matter device, salinity recovery unit, connects through pipeline and liquid pump between each device, and preprocessing device is: the water outlet of the high-salinity wastewater regulating tank 101 is connected with the water inlet of the COD degradation device 102 through a pipeline and a regulating tank lift pump 109. The water outlet of the COD degradation device 102 is connected to the softening and desiliconizing device 103 through a pipeline and a softening and desiliconizing device water inlet pump 110. The water outlet of the softening and silicon-removing device 103 is connected to the intermediate water tank 104 through a pipeline and an intermediate water pump 111. The sludge outlet of the softening and desiliconizing device 103 is pumped to the sludge treatment device A105. The outlet of the intermediate water basin 104 is connected to the ion exchange unit 106 via a pipe and an ion exchange unit inlet pump 112. The outlet of the ion exchange unit 106 is piped to a pre-treatment effluent tank 107. The ion exchange device 106 is provided with a regenerant addition device 108. The regenerated liquid is periodically discharged to the high-salinity wastewater adjusting tank 101.
The water resource recovery device is as follows: the outlet of the pretreatment effluent pool 107 is connected with a cartridge filter A201 through a pipeline and a reverse osmosis device inlet pump 210. The outlet of the cartridge filter a201 is connected to the reverse osmosis unit 202 via a pipe and a reverse osmosis high-pressure pump 211. The reverse osmosis device 202 is connected with the outlet of the antisludging agent feeding device 203 through a pipeline. The cleaning inlet and outlet of the reverse osmosis device 202 are respectively connected with the outlet and inlet of the chemical cleaning device A204 through pipelines. The water production port of the reverse osmosis unit 202 is connected to a reuse water tank 208 via a pipeline. The concentrate inlet of the reverse osmosis unit 202 is connected to the super concentrator 205 via a pipe and a super concentrator feed pump 207. The water production port of the super concentrator 205 is piped to the reuse water tank 208. The concentrate inlet of the super concentrator 205 is connected to a concentrate tank 209 via a pipe. The cleaning port of the super concentrator 205 is connected to the outlet and inlet of the chemical cleaning device B206, respectively.
The liquid phase quality separation device comprises: the outlet of the concentrated water tank 209 is connected with a security filter B301 through a pipeline and a nanofiltration device water inlet pump 305. The outlet of the security filter B301 is connected with a nanofiltration device 302 through a pipeline and a nanofiltration high-pressure pump 306. The nanofiltration device 302 is connected with an outlet of the scale inhibitor feeding device B303 through a pipeline. The cleaning inlet and outlet of the nanofiltration device 302 are respectively connected with the outlet and inlet of the chemical cleaning device C304 through pipelines. The water producing port of the nanofiltration device 302 is connected to the brine tank 307 through a pipeline. The concentrate inlet of the nanofiltration device 302 is connected to a nitrate water tank 308 through a pipeline.
The salinity recovery unit is: the outlet of the brine tank 307 is connected to the # 1 crystallization device 401 via a pipe and a water inlet pump 410 of the # 1 crystallization device. An evaporation condensate outlet is connected to a condensate water pool 405 through a pipeline and a No. 1 condensate water pump 413. The mother liquor discharge port is connected with a mother liquor pool 406 through a pipeline and a # 1 mother liquor pump 415. The nitrate water tank 308 is connected to the No. 2 crystallizing device 402 through a pipeline and a water inlet pump 411 of the No. 2 crystallizing device. The mother liquor discharge port is connected with the intermediate water tank 409 through a pipeline and a 2# mother liquor pump 416. The intermediate salt separated by the No. 2 crystallizing device 402 is sent to the No. 3 crystallizing device hot melting tank 404 through a conveyer belt. This example uses the evaporative condensate collected in condensate sump 405 to redissolve the salt. The outlet of the hot melt tank 404 of the 3# crystallization device is connected with the 3# crystallization device 403 through a pipeline and a 3# crystallization device water inlet pump 412. An evaporation condensate outlet of the No. 3 crystallizing device 403 is connected to a condensate water tank 405 through a pipeline and a No. 3 condensate water pump 414. The mother liquor discharge port discharges into the mother liquor tank 406 through a pipe and a # 3 mother liquor pump 417. The outlet of the mother liquor tank 406 is connected with a mother liquor solidification device 407 through a pipeline and a mother liquor solidification device water inlet pump 418. The cleaning ports of the 1# crystallization device 401, the 2# crystallization device 402, the 3# crystallization device 403, the 3# crystallization device hot melt tank 404 and the mother liquor solidification device 407 are respectively connected with the outlet and the inlet of a chemical cleaning device D408.
The depth purification device is: the outlet of the middle water tank 409 of the salinity recovery section is connected to the deep purification device 501 through a pipeline and a deep purification device water inlet pump 503, the water outlet of the deep purification device 501 is connected to the concentrated water tank 209 through a pipeline and a purification mother liquid pump 504, and the sludge outlet of the deep purification device 501 is pumped to the sludge treatment device B502.
The treatment process of the device of the embodiment in use comprises the following steps:
a pretreatment section:
A. homogenizing the high-salinity wastewater by a regulating reservoir, conveying the homogenized high-salinity wastewater to a pretreatment device, and carrying out combined reagent reaction to remove COD, total hardness, total alkalinity and SiO in the wastewater2The reaction sludge is conveyed to a sludge dewatering device, the effluent is conveyed to an intermediate water tank, the total hardness in the wastewater is further removed by ion resin exchange, the effluent is conveyed to a deep pretreatment effluent tank, the COD of the effluent is less than or equal to 50mg/L, and the total hardness is less than or equal to 5mg/L (CaCO)3Calculated as CaCO) and the total alkalinity is less than or equal to 10mg/L3Meter), SiO2≤30mg/L。
A water resource recovery section:
B. conveying the effluent of the deep pretreatment to a water resource recovery device, conveying the produced water to a reuse water pool for production and reuse, and conveying the concentrated water to a concentrated water pool, wherein the salt content of the concentrated water is 15%, and the desalination rate is more than or equal to 97%;
liquid phase mass separation:
C. conveying the concentrated water to a liquid-phase quality grading device to produce a strand of concentrated water (saline water) mainly containing monovalent salt and a strand of concentrated water (saltwater) mainly containing divalent salt, and respectively conveying the strands of concentrated water (saltwater) and the strands of concentrated water (saltwater) mainly containing divalent salt to a saline water pool 307 and a saltwater pool 308, wherein the rejection rate of divalent salt in a liquid-phase quality grading section is more than or equal to 98%;
a salinity recovery section:
D. conveying the brine to a 1# crystallization device 401 in a salinity recovery section, separating out a high-quality sodium chloride product, discharging an evaporation condensate into a condensate tank, discharging a small amount of mother liquor into a mother liquor tank, wherein the crystallization temperature of the 1# crystallization device 401 is 65-75 ℃, the salt yield is 95-98%, and the evaporation condensate yield is 95-98%;
E. conveying the saltwater to a 2# crystallizing device 402 in a salinity recovery section, separating sodium sulfate decahydrate, conveying mother liquor to an intermediate water tank 409 in the salinity recovery section, controlling the crystallization temperature of the 2# crystallizing device 402 to be-5 ℃, and re-dissolving intermediate salts such as sodium sulfate decahydrate and the like through evaporation condensate to form a solution, wherein the salt content is 20%, and the evaporation condensate is selected for dissolving the intermediate salts;
F. conveying the intermediate salt solution to a 3# crystallizing device 403 in a salt recovery section, separating salt such as anhydrous sodium sulfate and the like, discharging evaporation condensate into a condensate water tank, discharging a small amount of mother liquor into a mother liquor tank 406, wherein the crystallization temperature of the 3# crystallizing device 403 is 95-105 ℃, the salt yield is 95-98%, and the evaporation condensate yield is 95-98%;
a deep purification section:
G. the mother liquor in the middle water tank in the salinity recovery section is conveyed to a deep purification device, the mother liquor is returned to the concentrated water tank 209 after pollutant impurities are removed, and COD, total hardness, total alkalinity and SiO in the wastewater are treated by the deep purification section2The removal rate is 40% -60%;
H. and conveying the mother liquor to a mother liquor curing device, and performing safe landfill treatment after curing. When the mother liquor is discharged and intensively disposed, the mother liquor is conveyed to a discharging point.
Example two
The difference between this embodiment and the embodiment is that the position of the nanofiltration device 302 and the 2# crystallization device 402 in five devices including a pretreatment device, a water resource recovery device, a liquid phase quality separation device, a salinity recovery device, and a deep purification device are exchanged.
Taking the strong brine wastewater to be treated of a typical petrochemical zero discharge device as an example, the water inlet amount is 200m3And the salt content is 0.8 percent, wherein the main salts comprise sodium sulfate and sodium chloride, sulfate radical 3540mg/L, chlorine radical 1585mg/L, COD 300mg/L, total hardness 400mg/L, total alkalinity 190mg/L and soluble silicon 260mg/L, and after the high-salinity wastewater steady state recycling process is carried out, the yield of industrial salt is more than 95 percent and the yield of reuse water is more than 98 percent finally.
The treatment facility of this embodiment includes preprocessing device, water resource recovery unit, liquid phase branch matter device, salinity recovery unit, connects through pipeline and liquid pump between each device, and its characterized in that preprocessing device is: the water outlet of the high-salinity wastewater regulating tank 101 is connected with the water inlet of the COD degradation device 102 through a pipeline and a regulating tank lift pump 109, the water outlet of the COD degradation device 102 is connected to the softening and desiliconizing device 103 through a pipeline and a softening and desiliconizing device water inlet pump 110, the water outlet of the softening and desiliconizing device 103 is connected to the intermediate water tank 104 through a pipeline and an intermediate water pump 111, the sludge outlet of the softening and desiliconizing device 103 is pumped to a sludge treatment device A105, the water outlet of the intermediate water tank 104 is connected to an ion exchange device 106 through a pipeline and an ion exchange device water inlet pump 112, the water outlet of the ion exchange device 106 is connected to a pretreatment water outlet tank 107 through a pipeline, the ion exchange device 106 is provided with a regenerant adding device 108, and the regenerant.
The water resource recovery device is as follows: the water outlet of the pretreatment water outlet pool 107 is connected with a cartridge filter A201 through a pipeline and a reverse osmosis device water inlet pump 210, the outlet of the cartridge filter A201 is connected with a reverse osmosis device 202 through a pipeline and a reverse osmosis high-pressure pump 211, the reverse osmosis device 202 is connected with the outlet of a scale inhibitor feeding device A203 through a pipeline, the cleaning inlet and the cleaning outlet of the reverse osmosis device 202 are respectively connected with the outlet and the inlet of a chemical cleaning device A204 through pipelines, the water production port of the reverse osmosis device 202 is connected to a reuse water pool 208 through a pipeline, the concentrated water port of the reverse osmosis device 202 is connected with a super concentration device 205 through a pipeline and a super concentration device water inlet pump 207, the water production port of the super concentration device 205 is connected to the reuse water pool 208 through a pipeline, and the concentrated water port of the. The cleaning port of the super concentrator 205 is connected to the outlet and inlet of the chemical cleaning device B206, respectively.
The liquid phase quality separation device comprises: an outlet of a middle concentrated water tank 409 of the salinity recovery device is connected with a security filter B301 through a pipeline and a nanofiltration device water inlet pump 305, an outlet of the security filter B301 is connected with a nanofiltration device 302 through a pipeline and a nanofiltration high-pressure pump 306, the nanofiltration device 302 is connected with an outlet of a scale inhibitor feeding device B303 through a pipeline, a cleaning inlet and a cleaning outlet of the nanofiltration device 302 are respectively connected with an outlet and an inlet of a chemical cleaning device C304 through pipelines, a water production port of the nanofiltration device 302 is connected to the saline water tank 307 through a pipeline, and a concentrated water port of the nanofiltration device 302 is connected to a water tank 308 through a pipeline.
The salinity recovery unit is: an outlet of the brine tank 307 is connected to the No. 1 crystallization device 401 through a pipeline and a water inlet pump 410 of the No. 1 crystallization device, an evaporation condensate outlet is connected to a condensate tank 405 through a pipeline and a No. 1 condensate pump 413, a mother liquid discharge port is discharged into the mother liquid tank 406 through a pipeline and a No. 1 mother liquid pump 415, a concentrated water tank 209 is connected to the No. 2 crystallization device 402 through a pipeline and a water inlet pump 411 of the No. 2 crystallization device, a mother liquid discharge port is discharged into an intermediate water tank 409 through a pipeline and a No. 2 mother liquid pump 416, intermediate salt separated from a separation port of the No. 2 crystallization device is conveyed to a No. 3 crystallization device hot dissolving tank 404 through a conveying belt, and the evaporation condensate collected by the condensate tank 405 is adopted in the embodiment. An outlet of the 3# crystallization device hot melting tank 404 is connected to the 3# crystallization device 403 through a pipeline and a water inlet pump 412 of the 3# crystallization device, evaporation condensate is connected to a condensate water tank 405 through a pipeline and a 3# condensate water pump 414, a mother liquid outlet is connected to the mother liquid tank 406 through a pipeline and a 3# mother liquid pump 417, and an outlet of the mother liquid tank 406 is connected to a mother liquid solidification device 407 through a pipeline and a mother liquid solidification device water inlet pump 418. The cleaning ports of the 1# crystallization device 401, the 2# crystallization device 402, the 3# crystallization device 403, the 3# crystallization device hot melt tank 404 and the mother liquor solidification device 407 are respectively connected with the outlet and the inlet of a chemical cleaning device D408.
The depth purification device is: the outlet of the saltpeter pool 308 is connected to the deep purification device 501 through a pipeline and a deep purification device water inlet pump 503, the water outlet of the deep purification device 501 is connected to the concentrated water pool 209 through a pipeline and a purified mother liquor water outlet pump 504, and the sludge outlet of the deep purification device 501 is pumped to the sludge treatment device B502 through a pump.
The processing steps when using the processing apparatus of this embodiment are as follows:
A. homogenizing the high-salinity wastewater by a regulating reservoir, conveying the homogenized high-salinity wastewater to a pretreatment device, and carrying out combined reagent reaction to remove COD, total hardness, total alkalinity and SiO in the wastewater2The reaction sludge is conveyed to a sludge dewatering device, the effluent is conveyed to an intermediate water tank 104 in a pretreatment device, ion resin exchange is carried out to further remove the total hardness in the wastewater, the effluent is conveyed to a deep pretreatment effluent tank 107, the COD of the effluent is less than or equal to 30mg/L, and the total hardness is less than or equal to 1mg/L (CaCO is used)3Calculated as CaCO) and the total alkalinity is less than or equal to 5mg/L3Meter), SiO2≤20mg/L。
B. Conveying the effluent of the deep pretreatment to a water resource recovery device, conveying the produced water to a reuse water tank 209 for production and reuse, and conveying the concentrated water to a concentrated water tank, wherein the salt content of the concentrated water is 20%, and the desalination rate is more than or equal to 97%;
C. conveying the concentrated water to a No. 2 crystallizing device 402 in a salinity recovery section, separating sodium sulfate decahydrate, conveying the mother liquor to an intermediate water tank 409 in the salinity recovery section, controlling the crystallizing temperature of the No. 2 crystallizing device 402 to be 0 ℃, and re-dissolving intermediate salts such as sodium sulfate decahydrate and the like through evaporation condensate to form a solution, wherein the salt content is 20%, and the evaporation condensate is selected for dissolving the intermediate salts;
D. conveying the mother liquor in the intermediate water tank 409 in the salinity recovery section to a liquid-phase quality grading device to produce a strand of concentrated water (brine) mainly containing monovalent salt and a strand of concentrated water (saltwater) mainly containing divalent salt, and respectively conveying the strands of concentrated water (saltwater) to a brine tank 307 and a saltwater tank 308, wherein the retention rate of the liquid-phase quality grading section on the divalent salt is more than or equal to 96%;
E. conveying the saltpeter water to a deep purification device, removing pollutant impurities in the saltpeter water, returning the saltpeter water to a concentrated water tank 209, and carrying out deep purification on COD (chemical oxygen demand), total hardness, total alkalinity and SiO (silicon dioxide) in the wastewater2The removal rate is 50% -70%;
F. conveying the brine to a 1# crystallizing device 401 in a salinity recovery section, separating out a high-quality sodium chloride product, discharging an evaporation condensate into a condensate water tank 405, discharging a small amount of mother liquor into a mother liquor tank 406, wherein the crystallization temperature of the 1# crystallizing device 401 is 65-75 ℃, the salt yield is 95% -98%, and the evaporation condensate yield is 95% -98%;
G. conveying the intermediate salt solution to a 3# crystallization device 403 in a salt recovery section, separating salt such as anhydrous sodium sulfate and the like, discharging evaporation condensate into a condensate water tank 405, discharging a small amount of mother liquor into a mother liquor tank 406, wherein the crystallization temperature of the 3# crystallization device 403 is 95-105 ℃, the salt yield is 95-98%, and the evaporation condensate yield is 95-98%;
H. and conveying the mother liquor to a mother liquor curing device, and performing safe landfill treatment after curing. When the mother liquor is discharged and intensively disposed, the mother liquor is conveyed to a discharging point.
Claims (7)
1. The utility model provides a high salt waste water steady state resourceful device, divides matter device, salinity recovery unit, deep purification device including preprocessing device, water resource recovery unit, liquid phase, connects through pipeline and liquid pump between each device, and its characterized in that preprocessing device is: a water outlet of a high-salinity wastewater regulating tank (101) is connected with a water inlet of a COD degradation device (102) through a pipeline and a regulating tank lifting pump (109), a water outlet of the COD degradation device (102) is connected with a softening silicon removal device (103) through a pipeline and a softening silicon removal device water inlet pump (110), a water outlet of the softening silicon removal device (103) is connected with an intermediate water tank (104) through a pipeline and an intermediate water pump (111), a sludge outlet of the softening silicon removal device (103) is connected with a sludge treatment device A (105) through a pump, a water outlet of the intermediate water tank (104) is connected to an ion exchange device (106) through a pipeline and an ion exchange device water inlet pump (112), a water outlet of the ion exchange device is connected to a pretreatment water outlet tank (107) through a pipeline, the ion exchange device (106) is provided with a regenerant adding device (108), and a regenerated liquid is periodically discharged to the high-salinity wastewater regulating tank (;
the water resource recovery device is as follows: the water outlet of the pretreatment water outlet pool (107) is connected with a cartridge filter A (201) through a pipeline and a reverse osmosis device water inlet pump (210), the outlet of the cartridge filter A (201) is connected with a reverse osmosis device (202) through a pipeline and a reverse osmosis high-pressure pump (211), the reverse osmosis device (202) is connected with the outlet of a scale inhibitor feeding device A (203) through a pipeline, the cleaning inlet and the cleaning outlet of the reverse osmosis device (202) are respectively connected with the outlet and the inlet of a chemical cleaning device A (204) through pipelines, the water production port of the reverse osmosis device (202) is connected to a reuse water pool (208) through a pipeline, the concentrated water port of the reverse osmosis device (202) is connected with a super concentration device (205) through a pipeline and a super concentration device water inlet pump (207), the water production port of the super concentration device (205) is connected to a reuse water pool (208) through a pipeline, and the concentrated water port of the super concentration device (, the cleaning port of the super concentration device (205) is respectively connected with the outlet and the inlet of the chemical cleaning device B (206);
the liquid phase quality separation device comprises: an outlet of the concentrated water tank (209) is connected with a security filter B (301) through a pipeline and a nanofiltration device water inlet pump (305), an outlet of the security filter B (301) is connected with a nanofiltration device (302) through a pipeline and a nanofiltration high-pressure pump (306), the nanofiltration device (302) is connected with an outlet of a scale inhibitor feeding device B (303) through a pipeline, a cleaning inlet and a cleaning outlet of the nanofiltration device (302) are respectively connected with an outlet and an inlet of a chemical cleaning device C (304) through pipelines, a water production port of the nanofiltration device (302) is connected to a saline water tank (307) through a pipeline, and a concentrated water port of the nanofiltration device (302) is connected to a nitrate water tank (308) through a pipeline;
the salinity recovery unit is: an outlet of a brine tank (307) is connected to a No. 1 crystallization device (401) through a pipeline and a water inlet pump (410) of the No. 1 crystallization device, an evaporation condensate outlet is connected to a condensate tank (405) through a pipeline and a No. 1 condensate pump (413), a mother liquor discharge port is connected with a mother liquor tank (406) through a pipeline and a No. 1 mother liquor pump (415), a nitrate tank (308) is connected to a No. 2 crystallization device (402) through a pipeline and a water inlet pump (411) of the No. 2 crystallization device, a mother liquor discharge port is connected with an intermediate water tank (409) through a pipeline and a No. 2 mother liquor pump (416), intermediate salt separated from a separation outlet of the No. 2 crystallization device (402) is conveyed to a No. 3 crystallization device hot dissolving tank (404) through a conveying belt, the salt is dissolved back by the evaporation condensate collected by the condensate tank (405), an outlet of the No. 3 crystallization device hot dissolving tank (404) is connected to a No. 3 crystallization device (403) through a pipeline and a, an evaporation condensate outlet is connected to a condensate water tank (405) through a pipeline and a 3# condensate water pump (414), a mother liquor discharge port is connected with a mother liquor tank (406) through a pipeline and a 3# mother liquor pump (417), an outlet of the mother liquor tank (406) is connected with a mother liquor solidification device (407) through a pipeline and a mother liquor solidification device water inlet pump (418), and cleaning ports of a 1# crystallization device (401), a 2# crystallization device (402), a 3# crystallization device (403), a 3# crystallization device hot-melt pool (404) and a mother liquor solidification device (407) are respectively connected with an outlet and an inlet of a chemical cleaning device D (408);
the depth purification device is: the outlet of the salinity recovery intermediate water tank (409) is connected to the deep purification device (501) through a pipeline and a deep purification device water inlet pump (503), the water outlet of the deep purification device (501) is connected to the concentrated water tank (209) through a pipeline and a purified mother liquor water outlet pump (504), and the sludge outlet of the deep purification device (501) is pumped to the sludge treatment device B (502).
2. The high-salinity wastewater steady-state resource device according to claim 1, characterized in that the cation exchange resin of the ion exchange device (106) is a macroporous cation exchange resin suitable for divalent cation adsorption.
3. The steady state resource device for high salinity wastewater as defined in claim 1, characterized in that the reverse osmosis membrane of the reverse osmosis device (202) is an anti-pollution type brackish water membrane and an anti-pollution type sea fresh water membrane.
4. The steady-state recycling device for high-salinity wastewater according to claim 1, characterized in that the nanofiltration membrane of the nanofiltration device (302) is a high-precision mono-divalent separation nanofiltration membrane module.
5. The steady state resource device of high salinity wastewater according to claim 1, characterized in that the nanofiltration device (302) is exchanged with the 2# crystallization device (402), and the outlet of the concentrated water tank (209) is connected with the inlet of the 2# crystallization device (402) through a pipeline and a water inlet pump (411) of the 2# crystallization device.
6. The steady-state recycling device for high-salinity wastewater as claimed in claim 1, wherein the nano-filtration device (302) is exchanged with the 2# crystallization device (402), the outlet of the salinity recovery intermediate water tank (409) is connected with the security filter B (301) through a pipeline and a nano-filtration device water inlet pump (305), and the outlet of the security filter B (301) is connected with the nano-filtration device (302) through a pipeline and a nano-filtration high-pressure pump (306).
7. The steady-state recycling device for high-salinity wastewater as claimed in claim 1, wherein the nano-filtration device (302) is exchanged with the 2# crystallization device (402), the outlet of the saltwater pool (308) is connected with the deep purification device (501) through a pipeline and a deep purification device water inlet pump (503), and the outlet of the deep purification device (501) is connected with the inlet of the concentrated water pool (209) through a pipeline and a purified mother liquor water outlet pump (504).
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