CN206444229U - MVR evaporation and crystallization systems and industrial alkali waste liquid treating system - Google Patents
MVR evaporation and crystallization systems and industrial alkali waste liquid treating system Download PDFInfo
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Abstract
The utility model provides a kind of MVR evaporation and crystallization systems and industrial alkali waste liquid treating system, and the system includes：Pre-heating system, forced-circulation evaporation crystal system and steam circulation；Pre-heating system includes the feed pump and heat exchanger being connected；Forced-circulation evaporation crystal system includes forced circulation heater, crystallizing evaporator, mother liquor tank and the mother liquor reflux pump for passing sequentially through pipeline communication；Mother liquor reflux pump is connected by pipeline with forced circulation heater, and the discharge gate of heat exchanger is connected with crystallizing evaporator；Steam circulation includes vapour compression machine and motor；Vapour compression machine is connected with crystallizing evaporator and forced circulation heater respectively, the salkali waste liquid treating system, including pretreatment system, MVR evaporation and crystallization systems thickener and the centrifuge being connected；Pretreatment system drops to less than 10 to reduce COD value in spent lye, also, by the turbidity of spent lye, to reach MVR evaporation and crystallization system process demands.
Description
Technical field
The utility model is related to Industry Waste alkali lye process field, more particularly, to a kind of MVR evaporation and crystallization systems and industry
Salkali waste liquid treating system.
Background technology
High salt difficult degradation spent lye is produced in petroleum cracking workshop section, it is as follows that it produces process：
1. due to producing a large amount of H in oil gas2S by caustic scrubber (40%NaOH spent lye), it is necessary to be entered
Row washing, generates Na2S、Na2CO3And NaHCO3。
2. pass through O again2Oxidation generates Na2SO4、Na2SO3With a small amount of Na2CO3,
3. by adding H2SO4Excessive NaOH is neutralized, is finally produced as, Na2SO3、 Na2SO4With some impurity.
Because the original liquid component that finally produces is complicated, the COD not only containing about 5000ppm or so, and also TDS is up to 15%
More than.Technology for treating industrial waste water general at present, can not reach qualified discharge, and can not normally enter current dirt at all
Water treatment system, it is necessary to carry out advanced treating, at present, without good solution, can be handled spent lye, to reach
Cool back and use water national standard, and to salinity Na therein2SO4Crystallization carries out resource recycling.
Accordingly, it would be desirable to which one kind can handle this spent lye system in real time, the water of discharge is set to reach country's cooling recycle-water
Index, and will wherein valuable salinity Na2SO4Crystallization is reclaimed, and its purity reaches Na more than industrial second standard2SO4Knot
Crystalline substance, realizes that resource reclaim is recycled.
Utility model content
The purpose of this utility model is to provide a kind of MVR evaporation and crystallization systems and industrial alkali waste liquid treating system, to solve
Spent lye can not be certainly effectively treated present in prior art, water national standard is used to reach to cool back, and to wherein
Salinity Na2SO4The problem of crystallization carries out resource recycling.
The MVR evaporation and crystallization systems that the utility model is provided, including：Pre-heating system, forced-circulation evaporation crystal system and
Steam circulation；
The pre-heating system includes the feed pump and heat exchanger being connected；
The forced-circulation evaporation crystal system is returned including forced circulation heater, crystallizing evaporator, mother liquor tank and mother liquor
Flow pump；
The forced circulation heater is connected with crystallizing evaporator, and the crystallizing evaporator discharging opening is connected with thickener,
The thickener discharging opening is connected with seperator；
The mother liquor reflux pump intake is connected with seperator, and mother liquor reflux pump discharge passes through pipeline and forced circulation heater
Connection, the discharge gate of the heat exchanger is connected with crystallizing evaporator；
The steam circulation includes the motor of vapour compression machine and the driving vapour compression machine；
The vapour compression machine is connected with crystallizing evaporator and forced circulation heater respectively.
Further, the heat exchanger includes first-class heat exchanger and the secondary heat exchanger being connected, the secondary heat exchanger
Connected with crystallizing evaporator；
The first-class heat exchanger is on-condensible gas heat exchanger, and the secondary heat exchanger is steam condensate (SC) heat exchanger.
Further, spent lye with on-condensible gas heat exchanger by exchanging heat, and temperature rises to 32 DEG C by 25 DEG C, then spent lye
By being exchanged heat with steam condensate (SC) heat exchanger, temperature rises to 88 DEG C by 32 DEG C, to reach the temperature of crystallizing evaporator setting.
Further, crystallizing evaporator produces indirect steam and entered by pipeline in vapour compression machine, the both vapor compression
Machine does work to indirect steam, makes its temperature by 85 DEG C of liftings to 101 DEG C, and then circulation conveying is to forced circulation heater, with
Realize that the latent heat of indirect steam is recycled, the condensed water for finally making indirect steam condensation become 101 DEG C passes through condensed water
Pipeline is inputted into secondary heat exchanger.
Further, 88 DEG C of spent lye is continuously entered is flashed in crystallizing evaporator, and oversaturated sodium sulphate is steaming
Hair crystallizer is precipitated, and sedimentation time and the path of crystallization are precipitated by control, crystal is grown in crystallizing evaporator,
The larger crystallization of grain, which enters, eluriates leg, is detected using densitometer when meeting discharging condition, sequentially enters thickener, centrifuge,
Crystal is separated in rotation to centrifuge at a high speed, obtains the anhydrous slufuric acid sodium crystal of 5% moisture content；
The mother liquor that centrifuge comes out enters mother liquor tank, and mother liquor is delivered into crystallizing evaporator by pipeline by mother liquor reflux pump
Continue evaporative crystallization.
A kind of industrial alkali waste liquid treating system, including be connected pretreatment system, MVR evaporative crystallizations system as described above
System, thickener and seperator；
The pretreatment system drops to reduce COD value in spent lye to below 200ppm, also, by the turbidity of spent lye
To less than 10, to reach MVR evaporation and crystallization system process demands；
The MVR evaporation and crystallization systems to the spent lye to be evaporated crystallization, to separate out sodium sulfate crystal；
The thickener and seperator obtain anhydrous slufuric acid sodium crystal crystal to be separated from mixed liquor；
Also, the mother liquor being centrifuged out is delivered to MVR evaporation and crystallization systems and continues evaporative crystallization.
Further, the pretreatment system includes spent lye storage pipeline, feed pump, retort, acid solution tank, alkali lye
Tank, catalyst and oxidant tank, filter, cleaned water tank；
The feed pump stores pipeline by pipeline and spent lye respectively and retort is connected, and the feed pump will be that will give up
Alkali lye passes through in pipeline to retort；
The acid solution tank is mixed acid solution is delivered in spent lye storage pipeline by dosing pump with spent lye, to adjust
Save the acid-base value of spent lye；
Catalyst and the oxidant tank by dosing pump and retort by pipeline communication, to make spent lye and catalysis
Agent and oxidant carry out oxidation reaction under sour environment；
The outlet of the retort is connected by dehvery pump and pipe-and-filter, to reduce spent lye COD value and
Turbidity；
Pipeline between outlet and dehvery pump of the alkali liquid tank by dosing pump and pipeline with retort is connected, and is used to
Adjust the acid-base value of the spent lye of retort output；
The filter passes through pipeline and heat exchange by dehvery pump with the delivery port that purification water tank connects purification water tank
Device is connected.
Further, the spent lye in the feed pump is passed through with 8000kg/h regime flow and the sulfuric acid of 93% concentration
Pipeline is mixed to join retort.
Further, the filter is adsorbed to the COD in feed liquid, the COD value of spent lye to be reduced to
Below 200ppm, turbidity drops to less than 10.
Further, the pipeline phase between outlet and dehvery pump of the alkali liquid tank by dosing pump and pipeline with retort
Connection, to adjust retort output spent lye acid-base value to 8.
The MVR evaporation and crystallization systems that the utility model is provided are in thermal equilibrium state in evaporation stage system, it is not necessary to mend
Extra fresh steam is filled, the heat content that the indirect steam that system is produced in itself is compressed after heating through compressor disclosure satisfy that system is entered
The heat exchange balance of material, discharging and condensed water etc..
The operating cost of MVR evaporation and crystallization systems is than triple effect evaporator energy-conservation 50% or so.System that employs in system
Heat energy recycle and recycled back crystallizing evaporator, make the system have preferable energy-saving effect.
For above-mentioned industrial alkali waste liquid treating system, the system includes pretreatment system, MVR evaporation and crystallization systems, stiff
Device and seperator；Pretreatment system pre-processes skill to reduce COD values and turbidity in spent lye using advanced catalysis oxidation
Art, reduces influences of the COD of spent lye to subsequent technique, improves the purity of sodium sulphate in spent lye.
Brief description of the drawings
, below will be right in order to illustrate more clearly of the utility model embodiment or technical scheme of the prior art
The accompanying drawing used required in embodiment or description of the prior art is briefly described, it should be apparent that, describe below
In accompanying drawing be some embodiments of the present utility model, for those of ordinary skill in the art, do not paying creativeness
On the premise of work, other accompanying drawings can also be obtained according to these accompanying drawings.
The flow chart for the MVR evaporation and crystallization systems that Fig. 1 provides for the utility model embodiment；
The flow chart for the industrial alkali waste liquid treating system that Fig. 2 provides for the utility model embodiment；
The pretreatment system flow chart for the industrial alkali waste liquid treating system that Fig. 3 provides for the utility model embodiment；
The flow of the MVR evaporation and crystallization systems for the industrial alkali waste liquid treating system that Fig. 4 provides for the utility model embodiment
Figure.
Embodiment
The technical solution of the utility model is clearly and completely described below in conjunction with accompanying drawing, it is clear that described
Embodiment is a part of embodiment of the utility model, rather than whole embodiments.Based on the embodiment in the utility model, sheet
The every other embodiment that field those of ordinary skill is obtained under the premise of creative work is not made, belongs to this practicality
Novel protected scope.
, it is necessary to explanation in description of the present utility model, term " " center ", " on ", " under ", it is "left", "right", " perpendicular
Directly ", the orientation or position relationship of the instruction such as " level ", " interior ", " outer " are, based on orientation shown in the drawings or position relationship, to be only
Described for the ease of description the utility model and simplifying, rather than to indicate or imply that signified device or element must have specific
Orientation, with specific azimuth configuration and operation, therefore it is not intended that to limitation of the present utility model.In addition, term " the
One ", " second ", " the 3rd " are only used for describing purpose, and it is not intended that indicating or implying relative importance.
List below is the detection table that high salt difficult degradation spent lye is produced in petroleum cracking workshop section：
Table 1-1
The complete water quality analysis data of spent lye are directed to by above-mentioned list, it is known that：
Cation
Cation is with Na+Based on, average value is 5.8 × 104mg/L, accounts for the 99.99% of total cation, and other sun from
Son is only<0.01%；
Anion
Anion is with SO42-Based on, average value is 14.24 × 104mg/L, accounts for the 99.99% of total anion, and other are cloudy
Ion such as NO2-、NO3-、SO32-、S2O32-、Cl-Deng only<0.01%；
COD value
COD value changes between 3000-6000ppm.According to theory analysis, by measuring TOC value, it can calculate organic
Contribution of the thing to COD.In fact, reflect that the COD value of organic matter is only accounted between total COD value about 30%-40% in spent lye, and it is big
Part is the contribution with reducing substances, such as sulfide, SO3 2-、S2O3 2-Deng.
TDS values
TDS actual measurement scopes are 15.3*105-20.0*105ppm, are typical high-salt wastewater.
Total hardness
The excursion of total hardness numerical value is 91.9-149ppm, and the Ca surveyed2+With Mg2+It is converted into hardness number 21.11-
25.7ppm, difference is larger.After confirming with analysis personnel, learn that total hardness value is drawn through titration, and Ca2+、Mg2+Value is utilized
Spectroscopic methodology is drawn.Because water quality is complicated, to titration serious interference, influence very big, therefore, total hardness value deviation is larger, therefore with
Ca2+、Mg2+Hardness is reflected to be defined to consider technique.
Ph values
Ph values are 9, illustrate spent lye meta-alkalescence.
NH3-N values
The excursion of NH3-N values is 24.4-57.2ppm, illustrates that waste liquid ammonia nitrogen is changed greatly.
Sulfide
The excursion of sulfide value be 542-1480ppm, this explanation spent lye in preceding road oxidation technology some do not have
It is oxidized completely.Largely, it is also one of the reason for improving spent lye COD value.
Turbidity value
Turbidity value>100 degree, this explanation spent lye is muddy, and suspension and colloid substances are more.
Dissolved oxygen
The excursion of dissolved oxygen value is 4.35-4.5 × 103mg/L, is illustrated through in wet oxidation process, molten in spent lye
A large amount of oxygen are solved, wherein sulfide value is again higher, it was demonstrated that dissolved oxygen oxidation efficiency is not high.
After being analyzed and researched to spent lye water quality data, draw the following conclusions：
Spent lye water-quality constituents is more complicated.But mainly based on sodium sulphate, therefore, reclaim NaSO4 salt and realize recycling
It can be achieved on；
COD value is higher, and it can directly affect the long-time steady operation and industrial sulphuric acid sodium of follow-up MVR evaporation and crystallization systems
The purity of crystal.Therefore, spent lye is before MVR evaporative crystallization techniques are carried out, it is necessary to pre-processed, from effective processing
Technique reduces its COD value and turbidity.
Turbidity value>100, it is necessary to made up to before MVR evaporation and crystallization systems are entered less than 10.
Refer to the MVR evaporation and crystallization systems provided in Fig. 1, the present embodiment includes：Pre-heating system, forced-circulation evaporation knot
Crystallographic system is united and steam circulation；
The pre-heating system includes the feed pump and heat exchanger being connected；
The forced-circulation evaporation crystal system includes forced circulation heater, the evaporative crystallization for passing sequentially through pipeline communication
Device, mother liquor tank and mother liquor reflux pump；
The mother liquor reflux pump intake is connected with seperator, and mother liquor reflux pump discharge passes through pipeline and forced circulation heater
Connection, the discharge gate of the heat exchanger is connected with crystallizing evaporator；
The steam circulation includes the motor of vapour compression machine and the driving vapour compression machine；
The vapour compression machine is connected with crystallizing evaporator and forced circulation heater respectively.
Preferably, the heat exchanger in the present embodiment includes first-class heat exchanger and the secondary heat exchanger being connected, described two grades
Heat exchanger is connected with crystallizing evaporator；
The first-class heat exchanger is on-condensible gas heat exchanger, and the secondary heat exchanger is steam condensate (SC) heat exchanger.Raw material
Liquid is before crystallizing evaporator is entered, and its temperature requirement reaches the evaporating temperature of setting, it is therefore necessary to which feeding liquid is preheated.
In order to make full use of the heat energy of system, the spent lye with on-condensible gas heat exchanger by exchanging heat, and temperature rises to 32 DEG C by 25 DEG C,
Then spent lye with steam condensate (SC) heat exchanger by exchanging heat, and temperature rises to 88 DEG C by 32 DEG C, to reach that crystallizing evaporator is set
Temperature.
Preferably,
In view of evaporation efficiency and prevent the factor of calcium ions and magnesium ions easy fouling in evaporation tube, the steaming of design vapour compression machine
It is 85 degree to send out temperature.The cycle of calcium fouling can so be delayed.The system evaporating temperature is 85 DEG C, and waste liquid boiling point elevation value is about
9 DEG C, it is 8 ton hours to design total treating capacity.Consider investment and operation cost, using domestic centrifugal vapor compressor,
Vapour compression machine temperature rise selects 16 DEG C, and there is provided about 7 DEG C or so of effective temperature difference.
Crystallizing evaporator produces indirect steam and entered by pipeline in vapour compression machine, and the vapour compression machine steams to secondary
Vapour does work, and makes its temperature by 85 DEG C of liftings to 101 DEG C, then circulation conveying is to forced circulation heater, to realize secondary steaming
Recycling for the latent heat of vapour, finally makes indirect steam condensation become 101 DEG C of condensed waters, condensed water is inputted to two by pipeline
In level heat exchanger.
Because the outlet of vapour compression machine is superheated steam, by compressor outlet spray deionized water, reduction compression
Machine outlet temperature, finally gives saturated vapor.
88 DEG C of spent lye is continuously entered to be flashed in crystallizing evaporator, and oversaturated sodium sulphate is in crystallizing evaporator quilt
Separate out, sedimentation time and the path of crystallization are precipitated by control, crystal is grown in crystallizing evaporator, the larger knot of particle
Crystalline substance, which enters, eluriates leg, is detected using densitometer when meeting discharging condition, sequentially enters thickener, centrifuge, centrifuge is at a high speed
Crystal is separated in rotation, obtains the anhydrous slufuric acid sodium crystal of 5% moisture content；
The mother liquor that centrifuge comes out enters mother liquor tank, and mother liquor is delivered into crystallizing evaporator by pipeline by mother liquor reflux pump
Continue evaporative crystallization.
The MVR evaporation and crystallization systems that the utility model is provided are in thermal equilibrium state in evaporation stage system, it is not necessary to mend
Extra fresh steam is filled, the heat content that the indirect steam that system is produced in itself is compressed after heating through compressor disclosure satisfy that system is entered
The heat exchange balance of material, discharging and condensed water etc..
The operating cost of MVR evaporation and crystallization systems is than triple effect evaporator energy-conservation 50% or so.System that employs in system
Heat energy recycle and recycled back crystallizing evaporator, make the system have preferable energy-saving effect.
Reduction is needed in view of entering the COD value and turbidity of the spent lye in MVR evaporation and crystallization systems, figure is refer to
2 arrive Fig. 4, and the utility model additionally provides a kind of industrial alkali waste liquid treating system, and the system includes pretreatment system, above-mentioned
MVR evaporation and crystallization systems, thickener and seperator；
The pretreatment system drops to reduce COD value in spent lye to below 200ppm, also, by the turbidity of spent lye
To less than 10, to reach MVR evaporation and crystallization system process demands.
The MVR evaporation and crystallization systems to the spent lye to be evaporated crystallization, to separate out sodium sulfate crystal；
Refer to the pretreatment system in Fig. 4, this implementation includes spent lye storage pipeline, feed pump, retort, acid solution
Tank, alkali liquid tank, catalyst and oxidant tank, filter, cleaned water tank；
The feed pump stores pipeline by pipeline and spent lye respectively and retort is connected, and the feed pump will be that will give up
Alkali lye passes through in pipeline to retort；
The acid solution tank is mixed acid solution is delivered in spent lye storage pipeline by dosing pump with spent lye, to adjust
The acid-base value of spent lye is saved to 3.5；
Catalyst and the oxidant tank by dosing pump and retort by pipeline communication, to make spent lye and catalysis
Agent and oxidant carry out oxidation reaction under sour environment；
The outlet of the retort is connected by dehvery pump and pipe-and-filter, the COD value of spent lye to be reduced
To below 200ppm, turbidity drops to less than 10；
Pipeline between outlet and dehvery pump of the alkali liquid tank by dosing pump and pipeline with retort is connected, and is used to
The acid-base value of spent lye of retort output is adjusted to 8；The purpose of regulation acid-base value is allowed for into MVR evaporative crystallization techniques
The need for Ph values.
The filter is connected by dehvery pump with purification water tank.
The filler that filter is used, will adsorb to the COD in feed liquid, COD to below 200ppm can be reduced again,
Also turbidity is set to drop to less than 10 simultaneously.
A kind of industrial alkali waste liquid treating system that the utility model is provided, the system includes pretreatment system and MVR evaporates
Crystal system, thickener and seperator；
The pretreatment system drops to less than 10 to reduce COD value in spent lye, also, by the turbidity of spent lye, with
MVR evaporation and crystallization system process demands are reached, by MVR evaporation and crystallization systems to spent lye evaporative crystallization, improves and reclaims salkali waste
The purity of sodium sulphate in liquid；Recycle-water is cooled down simultaneously to be up to state standards；
MVR evaporation and crystallization systems reduce operating cost to be evaporated crystallization to the spent lye.
Finally it should be noted that：Various embodiments above is only limited to illustrate the technical solution of the utility model, rather than to it
System；Although the utility model is described in detail with reference to foregoing embodiments, one of ordinary skill in the art should
Understand：It can still modify to the technical scheme described in foregoing embodiments, or to which part or whole
Technical characteristic carries out equivalent substitution；And these modifications or replacement, the essence of appropriate technical solution is departed from this practicality newly
The scope of each embodiment technical scheme of type.
Claims (7)
1. a kind of MVR evaporation and crystallization systems, it is characterised in that including：Pre-heating system, forced-circulation evaporation crystal system and steam
The circulatory system；
The pre-heating system includes the feed pump and heat exchanger being connected；
The forced-circulation evaporation crystal system includes forced circulation heater, crystallizing evaporator, mother liquor tank and mother liquor reflux pump；
The forced circulation heater is connected with crystallizing evaporator, and the crystallizing evaporator discharging opening is connected with thickener, described
Thickener discharging opening is connected with seperator；
The mother liquor reflux pump intake is connected with seperator, and mother liquor reflux pump discharge is connected by pipeline and forced circulation heater
Logical, the discharge gate of the heat exchanger is connected with crystallizing evaporator；
The steam circulation includes the motor of vapour compression machine and the driving vapour compression machine；
The vapour compression machine is connected with crystallizing evaporator and forced circulation heater respectively.
2. MVR evaporation and crystallization systems according to claim 1, it is characterised in that the heat exchanger includes one be connected
Level heat exchanger and secondary heat exchanger, the secondary heat exchanger are connected with crystallizing evaporator；
The first-class heat exchanger is on-condensible gas heat exchanger, and the secondary heat exchanger is steam condensate (SC) heat exchanger.
3. a kind of industrial alkali waste liquid treating system, it is characterised in that including pretreatment system, such as claim 1-2 being connected
MVR evaporation and crystallization systems, thickener and seperator described in any one；
The pretreatment system drops to 10 to reduce COD value in spent lye to below 200ppm, also, by the turbidity of spent lye
Hereinafter, to reach MVR evaporation and crystallization system process demands；
The MVR evaporation and crystallization systems to the spent lye to be evaporated crystallization, to separate out sodium sulfate crystal；
The thickener and seperator obtain anhydrous slufuric acid sodium crystal crystal to be separated from mixed liquor；Also,
The mother liquor being centrifuged out is delivered to MVR evaporation and crystallization systems and continues evaporative crystallization.
4. industrial alkali waste liquid treating system according to claim 3, it is characterised in that the pretreatment system includes salkali waste
Liquid storage pipeline, feed pump, retort, acid solution tank, alkali liquid tank, catalyst and oxidant tank, filter, cleaned water tank；
The feed pump stores pipeline by pipeline and spent lye respectively and retort is connected, and the feed pump is to by spent lye
By in pipeline to retort；
The acid solution tank is mixed acid solution is delivered in spent lye storage pipeline by dosing pump with spent lye, useless to adjust
The acid-base value of alkali lye；
Catalyst and the oxidant tank by dosing pump and retort by pipeline communication, to make spent lye and catalyst and
Oxidant carries out oxidation reaction under sour environment；
The outlet of the retort is connected by dehvery pump and pipe-and-filter, COD value and turbidity to reduce spent lye；
Pipeline between outlet and dehvery pump of the alkali liquid tank by dosing pump and pipeline with retort is connected, to adjust
The acid-base value of the spent lye of retort output；
The filter passes through pipeline and heat exchanger phase by dehvery pump with the delivery port that purification water tank connects purification water tank
Connection.
5. industrial alkali waste liquid treating system according to claim 4, it is characterised in that spent lye in the feed pump with
8000kg/h regime flow and the sulfuric acid of 93% concentration are mixed to join retort by pipeline.
6. industrial alkali waste liquid treating system according to claim 4, it is characterised in that
The filter is adsorbed to the COD in feed liquid, the COD value of spent lye is reduced into below 200ppm, turbidity
Drop to less than 10.
7. industrial alkali waste liquid treating system according to claim 4, it is characterised in that the alkali liquid tank by dosing pump and
Pipeline between outlet and dehvery pump of the pipeline with retort is connected, the acid-base value of the spent lye to adjust retort output
To 8.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106587477A (en) * | 2016-12-21 | 2017-04-26 | 北京燕山翔宇环保工程技术有限公司 | System and method for treating industrial waste lye |
| CN108298569A (en) * | 2018-04-14 | 2018-07-20 | 上海中腾环保科技有限公司 | A kind of device and its production method producing hydronium(ion) lithia based on MVR |
| CN108439685A (en) * | 2018-04-14 | 2018-08-24 | 上海中腾环保科技有限公司 | A kind of sinker waste water treatment system and its processing method based on MVR evaporative crystallizations |
| WO2022041476A1 (en) * | 2020-08-31 | 2022-03-03 | 广东闻扬环境科技有限公司 | Salt-containing wastewater treatment apparatus |
-
2016
- 2016-12-21 CN CN201621421495.6U patent/CN206444229U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106587477A (en) * | 2016-12-21 | 2017-04-26 | 北京燕山翔宇环保工程技术有限公司 | System and method for treating industrial waste lye |
| CN108298569A (en) * | 2018-04-14 | 2018-07-20 | 上海中腾环保科技有限公司 | A kind of device and its production method producing hydronium(ion) lithia based on MVR |
| CN108439685A (en) * | 2018-04-14 | 2018-08-24 | 上海中腾环保科技有限公司 | A kind of sinker waste water treatment system and its processing method based on MVR evaporative crystallizations |
| WO2022041476A1 (en) * | 2020-08-31 | 2022-03-03 | 广东闻扬环境科技有限公司 | Salt-containing wastewater treatment apparatus |
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