CN105859003A - Method and device for salt separation and crystallization of high-salinity wastewater in coal chemical industry - Google Patents
Method and device for salt separation and crystallization of high-salinity wastewater in coal chemical industry Download PDFInfo
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- CN105859003A CN105859003A CN201610296561.XA CN201610296561A CN105859003A CN 105859003 A CN105859003 A CN 105859003A CN 201610296561 A CN201610296561 A CN 201610296561A CN 105859003 A CN105859003 A CN 105859003A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a method and a device for salt separation and crystallization of high-salinity wastewater in the coal chemical industry. The device comprises a first MVR (mechanical vapor recompression) forced evaporation unit, a cyclone separation filtering unit, a nanofiltration membrane group unit and a second MVR forced evaporation unit. The first MVR forced evaporation unit is used for evaporation of the high-salinity wastewater in the coal chemical industry to obtain sodium sulfate crystalline salt and first crystallization mother liquor; the cyclone separation filtering unit is used for removing tiny solid crystalline salt particles from the first crystallization mother liquor; the nanofiltration membrane group unit is used for removing divalent sulfate ions from the first crystallization mother liquor; the second MVR forced evaporation unit is used for evaporation and concentration of sodium chloride containing waste water to obtain sodium chloride crystalline salt and second crystallization mother liquor; the second MVR forced evaporation unit sends the second crystallization mother liquor into the nanofiltration membrane group unit to realize cyclic separation. The method and the device for salt separation and crystallization of the high-salinity wastewater in the coal chemical industry have advantages that low energy consumption, low cost and freeness of secondary pollution in treatment of the high-salinity wastewater are realized, resource recycling is realized as well, purity in salt separation and crystallization is greatly improved, and zero emission of wastewater is guaranteed.
Description
Technical field
The present invention relates to environmental technology field, divide salt-pepper noise particularly to a kind of Coal Chemical Industry high-salt wastewater
Device and method.
Background technology
China is a big coal country, Ye Shiyige Coal Chemical Industry big country.Substantial amounts of coal chemical industry enterprises produces
During can produce substantial amounts of high-salt wastewater discharge.In high-concentration salt-containing wastewater process field, often
The method using tradition multiple-effect evaporation processes.Tradition multiple-effect evaporation indirect steam cannot be fully utilized,
Energy-saving effect is not so good as MVR (mechanical steam recompression).Multiple-effect evaporation also needs to use circulating cooling
Water, increases cooling tower water consumption, the cost of power consumption.It addition, tradition multifunctional evaporating equipment quantity is many, account for
Ground area is big.At present, domestic relevant unit has carried out a point salt purification Technology's Study, substantially uses
Multiple-effect crystallisation step by step, actually remains as the differentiation of tradition evaporative crystallisation process, although can accomplish knot
Brilliant point of salt, but energy consumption still remains high.In terms of removing sulfate ion, activated coke is taked to adsorb
Or the mode adding calcium salt or barium salt removed.Activated coke suction type needs to regularly replace activated coke；
Add calcium salt or barium salt mode can introduce new carnallite in systems, be unfavorable for that follow-up crystallization divides salt.
Tradition evaporative crystallisation process energy consumption of the prior art is higher, and operating cost is high, and equipment takes up an area face
Long-pending big, it is impossible to avoid evaporimeter internal crystallization and fouling.
Summary of the invention
The invention provides a kind of Coal Chemical Industry high-salt wastewater and divide the device and method of salt-pepper noise, solve or
It is higher that part solves tradition evaporative crystallisation process energy consumption of the prior art, and operating cost is high, equipment
Floor space is big, it is impossible to avoid the technical problem of evaporimeter internal crystallization and fouling, it is achieved that low energy consumption,
Low cost, the processing high-salt wastewater and realize the recycling of resource of non-secondary pollution, increase substantially
The purity of crystallization point salt, it is ensured that the technique effect of wastewater zero discharge.
A kind of Coal Chemical Industry high-salt wastewater that the present invention provides divides the device of salt-pepper noise to include:
Oneth MVR forced evaporation unit, is used for evaporating described Coal Chemical Industry high-salt wastewater and produces concentrate,
Described concentrate crystallisation by cooling obtains sulfate crystal salt and the first crystalline mother solution；
Cyclonic separation filter element, is connected with a described MVR forced evaporation unit, is used for removing
The small solid grain of salt crystals contained in described first crystalline mother solution；
NF membrane group unit, is connected with described cyclonic separation filter element, is used for removing described first knot
Divalent sulfur acid ion in brilliant mother liquor, obtains sodium chloride-containing waste water；
2nd MVR forced evaporation unit, is connected with described NF membrane group unit, is used for being concentrated by evaporation
Described sodium chloride-containing waste water obtains sodium chloride crystal salt and the second crystalline mother solution；Described 2nd MVR is strong
Described second crystalline mother solution is sent into described NF membrane group unit and is circulated separation by evaporation element processed.
As preferably, described Coal Chemical Industry high-salt wastewater divides the device of salt-pepper noise also to include:
Pretreatment unit, for removing the mechanical admixture of described Coal Chemical Industry high-salt wastewater；
Described pretreatment unit is connected with a described MVR forced evaporation unit, will remove machinery miscellaneous
The described Coal Chemical Industry high-salt wastewater of matter sends into a described MVR forced evaporation unit.
As preferably, a described MVR forced evaporation unit and described 2nd MVR forced evaporation list
Unit is identical forced evaporation unit；
Described forced evaporation unit includes: water inlet tank, heat exchanger, forcing vaporiser, vapour compression machine,
Separator, cooler crystallizer, cyclone separator and centrifuge；
Described separator is connected with described water inlet tank by pipeline, and described heat exchanger is arranged on described pipeline
On；
Described separator is connected with described vapour compression machine, described vapour compression machine and described forced evaporation
Device connects；The outlet of described forcing vaporiser passes through described heat exchanger；
Described cooler crystallizer is connected with described separator, and institute sent into by the concentrate that described separator produces
State cooler crystallizer；
Described cooler crystallizer is connected with described cyclone separator；The mother liquor of described cyclone separator returns
Mouth is connected with described cooler crystallizer；
The outlet of described cyclone separator is connected with the entrance of described centrifuge.
As preferably, described forced evaporation unit also includes: feed pump, axial-flow pump and mother liquor pump；
Described feed pump is arranged on the pipeline between described separator and described water inlet tank, by described enter
Described Coal Chemical Industry high-salt wastewater in water pot sends into described separator；
Described forcing vaporiser is connected with described axial flow delivery side of pump, and the entrance of described axial-flow pump is with described
Separator connects；
Described mother liquor pump is arranged on the pipeline between described cooler crystallizer and described cyclone separator,
Liquid in described cooler crystallizer is sent into described cyclone separator.
As preferably, the water inlet tank in a described MVR forced evaporation unit connects described pretreatment
The outlet of unit；
Centrifuge in a described MVR forced evaporation unit is with described cyclonic separation filter element even
Connecing, described first crystalline mother solution is sent into described cyclonic separation filter element by described centrifuge；
The bypass outlet of described NF membrane group unit and entering in a described MVR forced evaporation unit
Water pot connects.
As preferably, described NF membrane group unit and entering in described 2nd MVR forced evaporation unit
Water pot connects, and described sodium chloride-containing waste water is sent into entering in described 2nd MVR forced evaporation unit
Water pot；
The bypass outlet of the centrifuge in described 2nd MVR forced evaporation unit and described NF membrane group
Unit connects, and described second crystalline mother solution is sent into described NF membrane group unit and is circulated separation.
As preferably, described heat exchanger is plate type heat exchanger；
Described forcing vaporiser is tubular heat exchanger or plate type heat exchanger.
The method that a kind of Coal Chemical Industry high-salt wastewater that the present invention provides divides salt-pepper noise, by described Coal Chemical Industry
High-salt wastewater divides the device of salt-pepper noise to realize, and comprises the following steps:
The mechanical admixture of described Coal Chemical Industry high-salt wastewater is removed by described pretreatment unit；
The described Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a described MVR forced evaporation
Unit is evaporated concentrating, and the concentrate crystallisation by cooling of generation obtains described sulfate crystal salt and described
First crystalline mother solution；
The small solid contained in described first crystalline mother solution is removed by described cyclonic separation filter element
Grain of salt crystals；
The divalent sulfur acid ion in described first crystalline mother solution is removed by described NF membrane group unit,
Obtain described sodium chloride-containing waste water；
It is evaporated concentrating by the described sodium chloride-containing waste water described 2nd MVR forced evaporation unit of feeding,
Obtaining described sodium chloride crystal salt and described second crystalline mother solution, described second crystalline mother solution returns to institute
State NF membrane group unit and be circulated separation.
As preferably, the technique of the described vapour compression machine in a described MVR forced evaporation unit
Parameter is: inlet pressure is 100KPa～120KPa；Outlet pressure is 150KPa～200KPa；
The technological parameter of the described vapour compression machine in described 2nd MVR forced evaporation unit is: enter
Mouth pressure is 58KPa～85KPa；Outlet pressure is 105KPa～148KPa.
As preferably, the technique of the described vapour compression machine in a described MVR forced evaporation unit
Parameter is: inlet pressure is 100KPa；Outlet pressure is 150KPa；
The technological parameter of the described vapour compression machine in described 2nd MVR forced evaporation unit is: enter
Mouth pressure is 70KPa；Outlet pressure is 125KPa.
One or more technical schemes provided herein, at least have the following technical effect that or advantage:
1, owing to have employed a MVR forced evaporation unit, cyclonic separation filter element, NF membrane
Group unit and the device of the 2nd MVR forced evaporation unit composition, package unit floor space is little, fortune
Row low cost；By the steaming in a MVR forced evaporation unit and the 2nd MVR forced evaporation unit
The principle that vapour compressor reuses after the indirect steam produced in evaporation compression being heated up, not only avoids
Use live steam, and thoroughly abandoned cooling tower, greatly reduce operating cost, it is achieved environmental protection
Energy-conservation, economize on water, saving expense；The separation being carried out divalent sulfur acid ion by NF membrane group unit is gone
Remove, the purity of crystallization point salt is greatly improved.Meanwhile, package unit can realize returning of crystalline mother solution
Stream, the mother liquor after separation returns to front end units and is circulated separation, the most outwardly discharges, it is ensured that thing
The multi-cycle separation of material, it is achieved wastewater zero discharge.So, efficiently solve tradition of the prior art to steam
Sending out method for crystallising energy consumption higher, operating cost is high, and occupation area of equipment is big, it is impossible in avoiding evaporimeter
Portion's crystallization and the technical problem of fouling, it is achieved that low energy consumption, low cost, the process height of non-secondary pollution
Salt waste water also realizes the recycling of resource, increases substantially the purity of crystallization point salt, it is ensured that waste water zero
The technique effect of discharge.
2, high owing to have employed the Coal Chemical Industry of MVR forced evaporation technology and Nanofiltration Membrane Separation Technology combination
Salt waste water divides the method for salt-pepper noise, MVR forced evaporation technology that Coal Chemical Industry high-salt wastewater is greatly lowered
Processing cost, Nanofiltration Membrane Separation Technology improves sodium sulphate and the purity of sodium chloride that crystallization obtains, logical
Cross the multi-cycle separation technique of design mother liquor, it is ensured that wastewater zero discharge.So, existing skill is efficiently solved
Traditional evaporative crystallisation process energy consumption in art is higher, it is impossible to avoid the skill of evaporimeter internal crystallization and fouling
Art problem, it is achieved that low energy consumption, low cost, the process high-salt wastewater of non-secondary pollution also realize resource
Recycling, increase substantially the purity of crystallization point salt, it is ensured that the technique effect of wastewater zero discharge.
Accompanying drawing explanation
Fig. 1 divides the configuration diagram of the device of salt-pepper noise for the Coal Chemical Industry high-salt wastewater that the present invention provides；
Fig. 2 divides the flow chart of the method for salt-pepper noise for the Coal Chemical Industry high-salt wastewater that the present invention provides.
Detailed description of the invention
The embodiment of the present application provides a kind of Coal Chemical Industry high-salt wastewater and divides the device and method of salt-pepper noise, solves
Determined or part to solve tradition evaporative crystallisation process energy consumption of the prior art higher, operating cost is high,
Occupation area of equipment is big, it is impossible to avoid the technical problem of evaporimeter internal crystallization and fouling, by arranging
Oneth MVR forced evaporation unit, cyclonic separation filter element, NF membrane group unit and the 2nd MVR
The Coal Chemical Industry high-salt wastewater of forced evaporation unit composition divides salt-pepper noise device, uses MVR forced evaporation
The Coal Chemical Industry high-salt wastewater that technology and Nanofiltration Membrane Separation Technology combine divides salt-pepper noise method to achieve low energy
Consumption, low cost, the processing high-salt wastewater and realize the recycling of resource, significantly of non-secondary pollution
Improve the purity of crystallization point salt, it is ensured that the technique effect of wastewater zero discharge.
Seeing accompanying drawing 1, a kind of Coal Chemical Industry high-salt wastewater that the present invention provides divides the device of salt-pepper noise to include:
Oneth MVR forced evaporation unit, cyclonic separation filter element, NF membrane group unit and the 2nd MVR
Forced evaporation unit.
Oneth MVR forced evaporation unit is used for evaporating Coal Chemical Industry high-salt wastewater and produces concentrate, concentrates
Liquid crystallisation by cooling obtains sulfate crystal salt and the first crystalline mother solution.Cyclonic separation filter element and first
MVR forced evaporation unit connects, for removing the small solid crystal salt contained in the first crystalline mother solution
Particle.NF membrane group unit is connected with cyclonic separation filter element, for removing in the first crystalline mother solution
Divalent sulfur acid ion, obtain sodium chloride-containing waste water.2nd MVR forced evaporation unit, and receives
Filter membrane group unit connects, and is used for being concentrated by evaporation sodium chloride-containing waste water and obtains sodium chloride crystal salt and the second knot
Brilliant mother liquor；Second crystalline mother solution is sent into NF membrane group unit and is carried out by the 2nd MVR forced evaporation unit
Multi-cycle separation.
Wherein, what vapour compression machine reused after the indirect steam produced in evaporation compression being heated up is former
Reason, not only avoids use live steam, and has thoroughly abandoned cooling tower, greatly reduce operation
Expense, be truly realized environmental protection and energy saving, economize on water, saving expense.This device can realize low energy consumption, low
Cost, the processing high-salt wastewater and realize the recycling of resource of non-secondary pollution, turn waste into wealth, from
And realize zero-emission truly.
Further, Coal Chemical Industry high-salt wastewater divides the device of salt-pepper noise also to include: pretreatment unit, uses
In the mechanical admixture removing Coal Chemical Industry high-salt wastewater；Pretreatment unit and a MVR forced evaporation list
Unit connects, and the Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a MVR forced evaporation unit.
Further, a MVR forced evaporation unit and the 2nd MVR forced evaporation unit are identical
Forced evaporation unit；Forced evaporation unit includes: water inlet tank, heat exchanger, forcing vaporiser, steaming
Vapour compressor, separator, cooler crystallizer, cyclone separator and centrifuge；Separator passes through pipeline
Being connected with water inlet tank, heat exchanger is arranged on pipeline；Separator is connected with vapour compression machine, vapour pressure
Contracting machine is connected with forcing vaporiser；The outlet of forcing vaporiser passes through heat exchanger；Cooler crystallizer with
Separator connects, and cooler crystallizer sent into by the concentrate that separator produces；Cooler crystallizer divides with eddy flow
Connect from device；The mother liquor return port of cyclone separator is connected with cooler crystallizer；Going out of cyclone separator
Mouth is connected with the entrance of centrifuge.
Further, forced evaporation unit also includes: feed pump, axial-flow pump and mother liquor pump；Feed pump
It is arranged on the pipeline between separator and water inlet tank, the Coal Chemical Industry high-salt wastewater in water inlet tank is sent into
Separator；Forcing vaporiser is connected with axial flow delivery side of pump, and the entrance of axial-flow pump is connected with separator；
Mother liquor pump is arranged on the pipeline between cooler crystallizer and cyclone separator, by cooler crystallizer
Liquid sends into cyclone separator.
Further, the water inlet tank in a MVR forced evaporation unit connects going out of pretreatment unit
Mouthful；Centrifuge in oneth MVR forced evaporation unit is connected with cyclonic separation filter element, centrifugal
First crystalline mother solution is sent into cyclonic separation filter element by machine；The bypass outlet of NF membrane group unit and
Water inlet tank in one MVR forced evaporation unit connects.
Further, the water inlet tank in NF membrane group unit and the 2nd MVR forced evaporation unit connects,
Sodium chloride-containing waste water is sent into the water inlet tank in the 2nd MVR forced evaporation unit；2nd MVR forces
The bypass outlet of the centrifuge in evaporation element is connected with NF membrane group unit, is sent by the second crystalline mother solution
Enter NF membrane group unit and be circulated separation.
Further, heat exchanger is plate type heat exchanger；Forcing vaporiser is tubular heat exchanger or board-like changes
Hot device.
See accompanying drawing 2, the method that a kind of Coal Chemical Industry high-salt wastewater that the present invention provides divides salt-pepper noise, logical
Crossing described Coal Chemical Industry high-salt wastewater divides the device of salt-pepper noise to realize, and comprises the following steps:
S1: removed the mechanical admixture of Coal Chemical Industry high-salt wastewater by pretreatment unit.
S2: the Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a MVR forced evaporation unit
Being evaporated concentrating, the concentrate crystallisation by cooling of generation obtains sulfate crystal salt and the first crystalline mother solution.
S3: removed the small solid crystallization contained in the first crystalline mother solution by cyclonic separation filter element
Salt particle.
S4: removed the divalent sulfur acid ion in the first crystalline mother solution by NF membrane group unit, obtain
Sodium chloride-containing waste water.
S5: be evaporated concentrating by sodium chloride-containing waste water feeding the 2nd MVR forced evaporation unit,
To sodium chloride crystal salt and the second crystalline mother solution, the second crystalline mother solution returns to NF membrane group unit to be carried out
Multi-cycle separation.
The method makes full use of MVR forced evaporation technology and Nanofiltration Membrane Separation Technology, thus significantly
Reduce the processing cost of Coal Chemical Industry high-salt wastewater, and make great efforts to improve sodium sulphate and the sodium chloride that crystallization obtains
Purity, thus realize zero-emission truly.
Further, the technological parameter of the vapour compression machine in a MVR forced evaporation unit is:
Inlet pressure is 100KPa～120KPa；Outlet pressure is 150KPa～200KPa；2nd MVR
The technological parameter of the vapour compression machine in forced evaporation unit is: inlet pressure is 58KPa～85KPa；
Outlet pressure is 105KPa～148KPa.As preferably, the steaming in a MVR forced evaporation unit
The technological parameter of vapour compressor is: inlet pressure is 100KPa；Outlet pressure is 150KPa；Second
The technological parameter of the vapour compression machine in MVR forced evaporation unit is: inlet pressure is 70KPa；Go out
Mouth pressure is 125KPa.
The Coal Chemical Industry high-salt wastewater provided the application with embodiment below in conjunction with the accompanying drawings divides salt-pepper noise method
It is described in detail.
Embodiment one
S1: flow is 1m3/ h, its total salinity, at the high-salt wastewater of 30000～15000mg/L, are led to
Cross pretreatment unit and remove the mechanical admixture of Coal Chemical Industry high-salt wastewater.
S2: the Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a MVR forced evaporation unit
Being evaporated concentrating, the concentrate crystallisation by cooling of generation obtains sulfate crystal salt and the first crystalline mother solution.
The technological parameter of the vapour compression machine in the oneth MVR forced evaporation unit is: inlet pressure is
105KPa；Outlet pressure is 160KPa.
S3: removed the small solid crystallization contained in the first crystalline mother solution by cyclonic separation filter element
Salt particle.
S4: removed the divalent sulfur acid ion in the first crystalline mother solution by NF membrane group unit, obtain
Sodium chloride-containing waste water.
S5: be evaporated concentrating by sodium chloride-containing waste water feeding the 2nd MVR forced evaporation unit,
To sodium chloride crystal salt and the second crystalline mother solution, the second crystalline mother solution returns to NF membrane group unit to be carried out
Multi-cycle separation.The technological parameter of the vapour compression machine in the 2nd MVR forced evaporation unit is: import
Pressure is 60KPa；Outlet pressure is 110KPa.
Embodiment two
S1: flow is 1m3/ h, its total salinity, at the high-salt wastewater of 30000～15000mg/L, are led to
Cross pretreatment unit and remove the mechanical admixture of Coal Chemical Industry high-salt wastewater.
S2: the Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a MVR forced evaporation unit
Being evaporated concentrating, the concentrate crystallisation by cooling of generation obtains sulfate crystal salt and the first crystalline mother solution.
The technological parameter of the vapour compression machine in the oneth MVR forced evaporation unit is: inlet pressure is
110KPa；Outlet pressure is 170KPa.
S3: removed the small solid crystallization contained in the first crystalline mother solution by cyclonic separation filter element
Salt particle.
S4: removed the divalent sulfur acid ion in the first crystalline mother solution by NF membrane group unit, obtain
Sodium chloride-containing waste water.
S5: be evaporated concentrating by sodium chloride-containing waste water feeding the 2nd MVR forced evaporation unit,
To sodium chloride crystal salt and the second crystalline mother solution, the second crystalline mother solution returns to NF membrane group unit to be carried out
Multi-cycle separation.The technological parameter of the vapour compression machine in the 2nd MVR forced evaporation unit is: import
Pressure is 65KPa；Outlet pressure is 115KPa.
Embodiment three
S1: flow is 1m3/ h, its total salinity, at the high-salt wastewater of 30000～15000mg/L, are led to
Cross pretreatment unit and remove the mechanical admixture of Coal Chemical Industry high-salt wastewater.
S2: the Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a MVR forced evaporation unit
Being evaporated concentrating, the concentrate crystallisation by cooling of generation obtains sulfate crystal salt and the first crystalline mother solution.
The technological parameter of the vapour compression machine in the oneth MVR forced evaporation unit is: inlet pressure is
115KPa；Outlet pressure is 180KPa.
S3: removed the small solid crystallization contained in the first crystalline mother solution by cyclonic separation filter element
Salt particle.
S4: removed the divalent sulfur acid ion in the first crystalline mother solution by NF membrane group unit, obtain
Sodium chloride-containing waste water.
S5: be evaporated concentrating by sodium chloride-containing waste water feeding the 2nd MVR forced evaporation unit,
To sodium chloride crystal salt and the second crystalline mother solution, the second crystalline mother solution returns to NF membrane group unit to be carried out
Multi-cycle separation.The technological parameter of the vapour compression machine in the 2nd MVR forced evaporation unit is: import
Pressure is 75KPa；Outlet pressure is 125KPa.
Embodiment four
S1: flow is 1m3/ h, its total salinity, at the high-salt wastewater of 30000～15000mg/L, are led to
Cross pretreatment unit and remove the mechanical admixture of Coal Chemical Industry high-salt wastewater.
S2: the Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a MVR forced evaporation unit
Being evaporated concentrating, the concentrate crystallisation by cooling of generation obtains sulfate crystal salt and the first crystalline mother solution.
The technological parameter of the vapour compression machine in the oneth MVR forced evaporation unit is: inlet pressure is
118KPa；Outlet pressure is 190KPa.
S3: removed the small solid crystallization contained in the first crystalline mother solution by cyclonic separation filter element
Salt particle.
S4: removed the divalent sulfur acid ion in the first crystalline mother solution by NF membrane group unit, obtain
Sodium chloride-containing waste water.
S5: be evaporated concentrating by sodium chloride-containing waste water feeding the 2nd MVR forced evaporation unit,
To sodium chloride crystal salt and the second crystalline mother solution, the second crystalline mother solution returns to NF membrane group unit to be carried out
Multi-cycle separation.The technological parameter of the vapour compression machine in the 2nd MVR forced evaporation unit is: import
Pressure is 80KPa；Outlet pressure is 135KPa.
Embodiment five
S1: flow is 1m3/ h, its total salinity, at the high-salt wastewater of 30000～15000mg/L, are led to
Cross pretreatment unit and remove the mechanical admixture of Coal Chemical Industry high-salt wastewater.
S2: the Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a MVR forced evaporation unit
Being evaporated concentrating, the concentrate crystallisation by cooling of generation obtains sulfate crystal salt and the first crystalline mother solution.
The technological parameter of the vapour compression machine in the oneth MVR forced evaporation unit is: inlet pressure is
102KPa；Outlet pressure is 195KPa.
S3: removed the small solid crystallization contained in the first crystalline mother solution by cyclonic separation filter element
Salt particle.
S4: removed the divalent sulfur acid ion in the first crystalline mother solution by NF membrane group unit, obtain
Sodium chloride-containing waste water.
S5: be evaporated concentrating by sodium chloride-containing waste water feeding the 2nd MVR forced evaporation unit,
To sodium chloride crystal salt and the second crystalline mother solution, the second crystalline mother solution returns to NF membrane group unit to be carried out
Multi-cycle separation.The technological parameter of the vapour compression machine in the 2nd MVR forced evaporation unit is: import
Pressure is 82KPa；Outlet pressure is 145KPa.
Sodium sulphate product and sodium chloride product that above-mentioned five embodiments obtain pass through detection, and sodium sulphate is brilliant
In body, sodium sulfate quality percentage is above 95%, and in sodium chloride crystal, sodium chloride mass percent is super
Cross 96%.
One or more technical schemes provided herein, at least have the following technical effect that or advantage:
1, owing to have employed a MVR forced evaporation unit, cyclonic separation filter element, NF membrane
Group unit and the device of the 2nd MVR forced evaporation unit composition, package unit floor space is little, fortune
Row low cost；By the steaming in a MVR forced evaporation unit and the 2nd MVR forced evaporation unit
The principle that vapour compressor reuses after the indirect steam produced in evaporation compression being heated up, not only avoids
Use live steam, and thoroughly abandoned cooling tower, greatly reduce operating cost, it is achieved environmental protection
Energy-conservation, economize on water, saving expense；The separation being carried out divalent sulfur acid ion by NF membrane group unit is gone
Remove, the purity of crystallization point salt is greatly improved.Meanwhile, package unit can realize returning of crystalline mother solution
Stream, the mother liquor after separation returns to front end units and is circulated separation, the most outwardly discharges, it is ensured that thing
The multi-cycle separation of material, it is achieved wastewater zero discharge.So, efficiently solve tradition of the prior art to steam
Sending out method for crystallising energy consumption higher, operating cost is high, and occupation area of equipment is big, it is impossible in avoiding evaporimeter
Portion's crystallization and the technical problem of fouling, it is achieved that low energy consumption, low cost, the process height of non-secondary pollution
Salt waste water also realizes the recycling of resource, increases substantially the purity of crystallization point salt, it is ensured that waste water zero
The technique effect of discharge.
2, high owing to have employed the Coal Chemical Industry of MVR forced evaporation technology and Nanofiltration Membrane Separation Technology combination
Salt waste water divides the method for salt-pepper noise, MVR forced evaporation technology that Coal Chemical Industry high-salt wastewater is greatly lowered
Processing cost, Nanofiltration Membrane Separation Technology improves sodium sulphate and the purity of sodium chloride that crystallization obtains, logical
Cross the multi-cycle separation technique of design mother liquor, it is ensured that wastewater zero discharge.So, existing skill is efficiently solved
Traditional evaporative crystallisation process energy consumption in art is higher, it is impossible to avoid the skill of evaporimeter internal crystallization and fouling
Art problem, it is achieved that low energy consumption, low cost, the process high-salt wastewater of non-secondary pollution also realize resource
Recycling, increase substantially the purity of crystallization point salt, it is ensured that the technique effect of wastewater zero discharge.
Above-described detailed description of the invention, enters the purpose of the present invention, technical scheme and beneficial effect
Go further description, be it should be understood that the specific embodiment party that the foregoing is only the present invention
Formula, is not limited to the present invention, all within the spirit and principles in the present invention, that is done appoints
What amendment, equivalent, improvement etc., should be included within the scope of the present invention.
Claims (10)
1. a Coal Chemical Industry high-salt wastewater divides the device of salt-pepper noise, it is characterised in that described Coal Chemical Industry is high
Salt waste water divides the device of salt-pepper noise to include:
Oneth MVR forced evaporation unit, is used for evaporating described Coal Chemical Industry high-salt wastewater and produces concentrate,
Described concentrate crystallisation by cooling obtains sulfate crystal salt and the first crystalline mother solution；
Cyclonic separation filter element, is connected with a described MVR forced evaporation unit, is used for removing
The small solid grain of salt crystals contained in described first crystalline mother solution；
NF membrane group unit, is connected with described cyclonic separation filter element, is used for removing described first knot
Divalent sulfur acid ion in brilliant mother liquor, obtains sodium chloride-containing waste water；
2nd MVR forced evaporation unit, is connected with described NF membrane group unit, is used for being concentrated by evaporation
Described sodium chloride-containing waste water obtains sodium chloride crystal salt and the second crystalline mother solution；Described 2nd MVR is strong
Described second crystalline mother solution is sent into described NF membrane group unit and is circulated separation by evaporation element processed.
2. Coal Chemical Industry high-salt wastewater as claimed in claim 1 divides the device of salt-pepper noise, it is characterised in that
Described Coal Chemical Industry high-salt wastewater divides the device of salt-pepper noise also to include:
Pretreatment unit, for removing the mechanical admixture of described Coal Chemical Industry high-salt wastewater；
Described pretreatment unit is connected with a described MVR forced evaporation unit, will remove machinery miscellaneous
The described Coal Chemical Industry high-salt wastewater of matter sends into a described MVR forced evaporation unit.
3. Coal Chemical Industry high-salt wastewater as claimed in claim 2 divides the device of salt-pepper noise, it is characterised in that
A described MVR forced evaporation unit and described 2nd MVR forced evaporation unit are identical
Forced evaporation unit；
Described forced evaporation unit includes: water inlet tank, heat exchanger, forcing vaporiser, vapour compression machine,
Separator, cooler crystallizer, cyclone separator and centrifuge；
Described separator is connected with described water inlet tank by pipeline, and described heat exchanger is arranged on described pipeline
On；
Described separator is connected with described vapour compression machine, described vapour compression machine and described forced evaporation
Device connects；The outlet of described forcing vaporiser passes through described heat exchanger；
Described cooler crystallizer is connected with described separator, and institute sent into by the concentrate that described separator produces
State cooler crystallizer；
Described cooler crystallizer is connected with described cyclone separator；The mother liquor of described cyclone separator returns
Mouth is connected with described cooler crystallizer；
The outlet of described cyclone separator is connected with the entrance of described centrifuge.
4. Coal Chemical Industry high-salt wastewater as claimed in claim 3 divides the device of salt-pepper noise, it is characterised in that
Described forced evaporation unit also includes: feed pump, axial-flow pump and mother liquor pump；
Described feed pump is arranged on the pipeline between described separator and described water inlet tank, by described enter
Described Coal Chemical Industry high-salt wastewater in water pot sends into described separator；
Described forcing vaporiser is connected with described axial flow delivery side of pump, and the entrance of described axial-flow pump is with described
Separator connects；
Described mother liquor pump is arranged on the pipeline between described cooler crystallizer and described cyclone separator,
Liquid in described cooler crystallizer is sent into described cyclone separator.
5. Coal Chemical Industry high-salt wastewater as claimed in claim 3 divides the device of salt-pepper noise, it is characterised in that
Water inlet tank in a described MVR forced evaporation unit connects the outlet of described pretreatment unit；
Centrifuge in a described MVR forced evaporation unit is with described cyclonic separation filter element even
Connecing, described first crystalline mother solution is sent into described cyclonic separation filter element by described centrifuge；
The bypass outlet of described NF membrane group unit and entering in a described MVR forced evaporation unit
Water pot connects.
6. Coal Chemical Industry high-salt wastewater as claimed in claim 3 divides the device of salt-pepper noise, it is characterised in that
Described NF membrane group unit is connected with the water inlet tank in described 2nd MVR forced evaporation unit,
Described sodium chloride-containing waste water is sent into the water inlet tank in described 2nd MVR forced evaporation unit；
The bypass outlet of the centrifuge in described 2nd MVR forced evaporation unit and described NF membrane group
Unit connects, and described second crystalline mother solution is sent into described NF membrane group unit and is circulated separation.
7. Coal Chemical Industry high-salt wastewater as claimed in claim 3 divides the device of salt-pepper noise, it is characterised in that
Described heat exchanger is plate type heat exchanger；
Described forcing vaporiser is tubular heat exchanger or plate type heat exchanger.
8. the method that Coal Chemical Industry high-salt wastewater divides salt-pepper noise, by any one of claim 1～7
Described Coal Chemical Industry high-salt wastewater divides the device of salt-pepper noise to realize, it is characterised in that comprise the following steps:
The mechanical admixture of described Coal Chemical Industry high-salt wastewater is removed by described pretreatment unit；
The described Coal Chemical Industry high-salt wastewater removing mechanical admixture is sent into a described MVR forced evaporation
Unit is evaporated concentrating, and the concentrate crystallisation by cooling of generation obtains described sulfate crystal salt and described
First crystalline mother solution；
The small solid contained in described first crystalline mother solution is removed by described cyclonic separation filter element
Grain of salt crystals；
The divalent sulfur acid ion in described first crystalline mother solution is removed by described NF membrane group unit,
Obtain described sodium chloride-containing waste water；
It is evaporated concentrating by the described sodium chloride-containing waste water described 2nd MVR forced evaporation unit of feeding,
Obtaining described sodium chloride crystal salt and described second crystalline mother solution, described second crystalline mother solution returns to institute
State NF membrane group unit and be circulated separation.
9. the method that Coal Chemical Industry high-salt wastewater as claimed in claim 8 divides salt-pepper noise, it is characterised in that
The technological parameter of the described vapour compression machine in a described MVR forced evaporation unit is: enter
Mouth pressure is 100KPa～120KPa；Outlet pressure is 150KPa～200KPa；
The technological parameter of the described vapour compression machine in described 2nd MVR forced evaporation unit is: enter
Mouth pressure is 58KPa～85KPa；Outlet pressure is 105KPa～148KPa.
10. the method that Coal Chemical Industry high-salt wastewater as claimed in claim 8 divides salt-pepper noise, its feature exists
In,
The technological parameter of the described vapour compression machine in a described MVR forced evaporation unit is: enter
Mouth pressure is 100KPa；Outlet pressure is 150KPa；
The technological parameter of the described vapour compression machine in described 2nd MVR forced evaporation unit is: enter
Mouth pressure is 70KPa；Outlet pressure is 125KPa.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107902677A (en) * | 2016-12-12 | 2018-04-13 | 威立雅水处理技术公司 | The method that potassium sulfate and sodium chloride are produced from waste water |
| CN108079607A (en) * | 2017-12-25 | 2018-05-29 | 合肥恒力装备有限公司 | A kind of evaporative crystallization anti-block apparatus |
| CN109896538A (en) * | 2019-03-28 | 2019-06-18 | 中国中轻国际工程有限公司 | A kind of evaporation of mechanical compression separates salt made from earth containing a comparatively high percentage of sodium chloride production technology with back dissolving |
| CN110702484A (en) * | 2019-11-11 | 2020-01-17 | 西南石油大学 | Method for calculating in-situ porosity and establishing water saturation of water-containing dissolved salt reservoir core |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120279847A1 (en) * | 2007-07-24 | 2012-11-08 | Brad Michael Malatesta | Method of cleaning and recycling glycol-tainted water from de-icing operations at airports |
| CN103172088A (en) * | 2013-04-11 | 2013-06-26 | 南风化工集团股份有限公司 | Application of MVR (mechanical vapor recompression) crystallizing evaporator in sodium sulfate and sodium chloride separation technology |
| CN103936220A (en) * | 2014-05-06 | 2014-07-23 | 田晓良 | Zero discharge treatment process of saline sewage produced by refining |
| CN104591464A (en) * | 2015-02-03 | 2015-05-06 | 石家庄工大化工设备有限公司 | Recycling method of high-salinity wastewater |
| CN104961285A (en) * | 2015-06-30 | 2015-10-07 | 石家庄工大化工设备有限公司 | Method for recycling high-salt waste water containing sodium chloride and sodium sulfate |
| CN104973726A (en) * | 2015-06-30 | 2015-10-14 | 石家庄工大化工设备有限公司 | Recovery processing method of high salinity wastewater containing sodium chloride and sodium sulfate |
| CN104986910A (en) * | 2015-07-23 | 2015-10-21 | 江苏德邦工程有限公司 | Mechanical steam recompression falling film evaporation process method and system |
| CN205099538U (en) * | 2015-11-02 | 2016-03-23 | 海洲环保集团有限公司 | High concentration contains salt waste water MVR evaporation crystallization process system |
| CN205856227U (en) * | 2016-05-06 | 2017-01-04 | 武汉宏澳绿色能源工程有限责任公司 | A kind of Coal Chemical Industry high-salt wastewater divides the device of salt-pepper noise |
-
2016
- 2016-05-06 CN CN201610296561.XA patent/CN105859003A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120279847A1 (en) * | 2007-07-24 | 2012-11-08 | Brad Michael Malatesta | Method of cleaning and recycling glycol-tainted water from de-icing operations at airports |
| CN103172088A (en) * | 2013-04-11 | 2013-06-26 | 南风化工集团股份有限公司 | Application of MVR (mechanical vapor recompression) crystallizing evaporator in sodium sulfate and sodium chloride separation technology |
| CN103936220A (en) * | 2014-05-06 | 2014-07-23 | 田晓良 | Zero discharge treatment process of saline sewage produced by refining |
| CN104591464A (en) * | 2015-02-03 | 2015-05-06 | 石家庄工大化工设备有限公司 | Recycling method of high-salinity wastewater |
| CN104961285A (en) * | 2015-06-30 | 2015-10-07 | 石家庄工大化工设备有限公司 | Method for recycling high-salt waste water containing sodium chloride and sodium sulfate |
| CN104973726A (en) * | 2015-06-30 | 2015-10-14 | 石家庄工大化工设备有限公司 | Recovery processing method of high salinity wastewater containing sodium chloride and sodium sulfate |
| CN104986910A (en) * | 2015-07-23 | 2015-10-21 | 江苏德邦工程有限公司 | Mechanical steam recompression falling film evaporation process method and system |
| CN205099538U (en) * | 2015-11-02 | 2016-03-23 | 海洲环保集团有限公司 | High concentration contains salt waste water MVR evaporation crystallization process system |
| CN205856227U (en) * | 2016-05-06 | 2017-01-04 | 武汉宏澳绿色能源工程有限责任公司 | A kind of Coal Chemical Industry high-salt wastewater divides the device of salt-pepper noise |
Non-Patent Citations (1)
| Title |
|---|
| 侯立安主编: "《小型污水处理与回用技术及装置》", 31 January 2003 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107902677A (en) * | 2016-12-12 | 2018-04-13 | 威立雅水处理技术公司 | The method that potassium sulfate and sodium chloride are produced from waste water |
| US10773969B1 (en) | 2016-12-12 | 2020-09-15 | Veolia Water Technologies, Inc. | Method for producing potassium sulfate and sodium chloride from wastewater |
| CN108079607A (en) * | 2017-12-25 | 2018-05-29 | 合肥恒力装备有限公司 | A kind of evaporative crystallization anti-block apparatus |
| CN109896538A (en) * | 2019-03-28 | 2019-06-18 | 中国中轻国际工程有限公司 | A kind of evaporation of mechanical compression separates salt made from earth containing a comparatively high percentage of sodium chloride production technology with back dissolving |
| CN110702484A (en) * | 2019-11-11 | 2020-01-17 | 西南石油大学 | Method for calculating in-situ porosity and establishing water saturation of water-containing dissolved salt reservoir core |
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