CN106587477A - System and method for treating industrial waste lye - Google Patents
System and method for treating industrial waste lye Download PDFInfo
- Publication number
- CN106587477A CN106587477A CN201611194122.4A CN201611194122A CN106587477A CN 106587477 A CN106587477 A CN 106587477A CN 201611194122 A CN201611194122 A CN 201611194122A CN 106587477 A CN106587477 A CN 106587477A
- Authority
- CN
- China
- Prior art keywords
- spent lye
- heat exchanger
- crystallization
- pipeline
- crystallizing evaporator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/18—Dehydration
-
- 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
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
Abstract
The invention provides a system and method for treating industrial waste lye. The method comprises the steps: carrying out pretreatment on the waste lye, so as to lower the COD value and turbidity of the waste lye; carrying out evaporative crystallization on the liquid mixture by using an MVR evaporative crystallization system; and separating crystals from the liquid mixture by using a thickener and a separator, and conveying centrifuged mother liquor to the MVR evaporative crystallization system for continuous evaporative crystallization. The system comprises a pretreatment system and the MVR evaporative crystallization system, wherein the pretreatment system is used for lowering the COD value and turbidity of the waste lye; the MVR evaporative crystallization system is used for carrying out evaporative crystallization on the waste lye; and crystals are separated from the liquid mixture by the thickener and the separator, and the centrifuged mother liquor is conveyed to the MVR evaporative crystallization system for continuous evaporative crystallization. The waste lye can be effectively treated so as to reach the national standards for cooled reuse water, and a saline matter, i.e., sodium sulfate crystals in the waste lye can be subjected to resource recycling.
Description
Technical field
The present invention relates to Industry Waste alkali liquor process field, more particularly, to a kind of industrial alkali waste liquid treating system and method.
Background technology
High salt difficult degradation spent lye is produced in petroleum cracking workshop section, it is as follows which produces process：
1. as a large amount of H are produced in oil gas2S, needs to enter by caustic scrubber (spent lye of 40%NaOH)
Row washing, generates Na2S、Na2CO3And NaHCO3。
2. O is passed through again2Oxidation generates Na2SO4、Na2SO3With a small amount of Na2CO3,
3. by adding H2SO4The excessive NaOH of neutralization, is finally produced as, Na2SO3、Na2SO4With some impurity.
Due to the final original liquid component for producing it is complicated, the COD not only containing about 5000ppm or so, and TDS up to 15% with
On.Technology for treating industrial waste water general at present, can not reach qualified discharge at all, and cannot normally enter current sewage
Processing system, it is necessary to carry out advanced treating, at present, no good solution can be processed to spent lye, cold to reach
But recycle-water national standard, and to salinity Na therein2SO4Crystallization carries out resource recycling.
Accordingly, it would be desirable to one kind can make the water of discharge reach national cooling with this spent lye method and system of real-time processing
Recycle-water index, and will wherein valuable salinity Na2SO4Crystallization is reclaimed, and its purity reaches more than industrial second standard
Na2SO4Crystallization, realizes that resource reclaim is recycled.
The content of the invention
It is an object of the invention to provide a kind of industrial alkali waste liquid treating system and method and system, to solve prior art
Present in spent lye can not be effectively treated, use water national standard to reach to cool back, and to salinity Na therein2SO4
Crystallization carries out the problem of resource recycling.
The industrial alkali waste liquid processing method that the present invention is provided, comprises the following steps：
Step 1, carries out pretreatment to spent lye, to reduce the COD value and turbidity of spent lye；
Step 1.1, adjusts the Ph values of spent lye；
Step 1.2, the spent lye in feed pump are added to retort by pipe-line mixer with acid solution, so that mixed liquor
Oxidation reaction is stably carried out under sour environment, the COD value of spent lye is reduced；
The Ph values of the mixed liquor after oxidation processes are adjusted to 8 by step 1.3；
Step 1.4, using the filler in filter, adsorbs to the COD in mixed liquor, makes the COD of mixed liquor
Below 200ppm is down to, while making turbidity drop to less than 10；
Step 2, is evaporated crystallization using MVR evaporation and crystallization systems to mixed liquor, to separate out sodium sulfate crystal；
Crystal is separated from mixed liquor by step 3 using thickener and seperator, obtains anhydrous sodium sulfate brilliant
Body；Also, the mother solution being centrifuged out is delivered to into MVR evaporation and crystallization systems and continues evaporative crystallization.
Further, sulphuric acid of the spent lye in the feed pump with the regime flow of 8000kg/h with 93% concentration passes through
Pipe-line mixer is added to retort.
Further, the step 2 comprises the steps：
Step 2.1, is preheated to mixed liquor using heat exchanger；
Step 2.2, is evaporated to the crystallizing evaporator that pre-warmed mixed liquor is delivered in MVR evaporation and crystallization systems
Crystallization treatment；
Step 2.3, is compressed process to the indirect steam that crystallizing evaporator is discharged, and to lift vapor (steam) temperature, then will
Steam is conveyed to the vapour compression machine in MVR evaporation and crystallization systems, to realize recycling for the latent heat of indirect steam, while will
The condensed water that forced circulation heater is discharged is input into into heat exchanger to preheat mixed liquor.
A kind of industrial alkali waste liquid treating system, including the pretreatment system, MVR evaporation and crystallization systems, thickener that are connected
And seperator；
The pretreatment system is to reduce in spent lye COD value to below 200ppm, also, the turbidity of spent lye is dropped
To less than 10, to reach MVR evaporation and crystallization system process demands；
The MVR evaporation and crystallization systems to be evaporated crystallization to the spent lye, to separate out sodium sulfate crystal；
The thickener and seperator obtain anhydrous slufuric acid sodium crystal crystal is separated from mixed liquor；
Also, the mother solution being centrifuged out is delivered to into 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 liquor
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 giving up
Alkali liquor is by pipeline to retort；
The acid solution tank is mixed with spent lye in pipeline acid solution to be delivered to spent lye and be stored by dosing pump, to adjust
The acid-base value of section spent lye；
The catalyst and oxidant tank pass through pipeline communication with retort by dosing pump, to make spent lye with catalysis
Agent and oxidant carry out oxidation reaction under sour environment；
The outlet of the retort passes through dehvery pump and pipe-and-filter is connected, and reduces to the COD value by spent lye
To below 200ppm, turbidity drops to less than 10；
The alkali liquid tank is connected by the pipeline between the outlet of dosing pump and pipeline and retort and dehvery pump, to
Adjust the acid-base value of the spent lye of retort output；
The filter is connected with purification water tank by dehvery pump.
Further, the MVR evaporation and crystallization systems include：Pre-heating system, forced-circulation evaporation crystal system and steam
Blood circulation；
The pre-heating system includes the feed pump being connected and heat exchanger；
The forced-circulation evaporation crystal system includes that forced circulation heater, crystallizing evaporator, mother liquor tank and mother solution are returned
Stream pump；
The forced circulation heater is connected with crystallizing evaporator, and the vaporizer 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 by pipeline and forced circulation heater
Connection, the discharge gate of the heat exchanger are connected with crystallizing evaporator；
The steam circulation includes vapour compression machine and drives the motor of the vapour compression machine；
The vapour compression machine is connected with crystallizing evaporator and forced circulation heater respectively.
Further, the heat exchanger includes the first-class heat exchanger being connected and secondary heat exchanger, the secondary heat exchanger
Connect 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, by exchanging heat with on-condensible gas heat exchanger, temperature rises to 32 DEG C by 25 DEG C, then gives up the spent lye
By exchanging heat with steam condensate (SC) heat exchanger, temperature rises to 88 DEG C by 32 DEG C to alkali liquor, to reach the temperature of crystallizing evaporator setting.
Further, crystallizing evaporator is produced indirect steam and is entered in vapour compression machine by pipeline, the both vapor compression
Machine does work to indirect steam so as to temperature lifted to 101 DEG C by 85 DEG C, then circulation conveying is to forced circulation heater, with
Realize that the latent heat of indirect steam is recycled, condensed water is passed through by the condensed water for finally making indirect steam condensation become 101 DEG C
Pipeline is input into into secondary heat exchanger.
Further, 88 DEG C of spent lye is continuously entered, and oversaturated sodium sulfate is steaming
Send out crystallizer to be precipitated, sedimentation time and the path of crystallization are precipitated by control, crystal is grown in crystallizing evaporator,
The larger crystallization of grain is entered eluriates lower limb, is detected using densimeter when meeting discharging condition, sequentially enters thickener, centrifuge,
Separated by rotation at a high speed by crystal for centrifuge, obtains the anhydrous slufuric acid sodium crystal of 5% moisture content；
Centrifuge mother solution out enters mother liquor tank, mother solution is delivered to crystallizing evaporator by pipeline by mother liquor reflux pump
Continue evaporative crystallization.
Based on the industrial alkali waste liquid processing method that above-mentioned technical proposal is provided：
Using catalysis oxidation preconditioning technique, spent lye is effectively treated, the COD of spent lye is reduced to subsequent technique
Impact, improve reclaim spent lye in sodium sulfate purity；
Cool down recycle-water simultaneously to be up to state standards；
Using the energy-efficient evaporation and crystallization systems of MVR (than two-effect evaporation device energy-conservation more than 70%), relatively low operation into is realized
This.
For a kind of industrial alkali waste liquid treating system that above-mentioned processing method, the present invention are provided, the system includes pretreatment
System and MVR evaporation and crystallization systems, thickener and seperator；
The pretreatment system is to reduce COD value in spent lye, also, the turbidity of spent lye is dropped to less than 10, with
MVR evaporation and crystallization system process demands are reached, by MVR evaporation and crystallization systems to spent lye evaporative crystallization, is improved and is reclaimed salkali waste
The purity of sodium sulfate in liquid；Cool down recycle-water simultaneously to be up to state standards；
MVR evaporation and crystallization systems reduce operating cost to be evaporated crystallization to the spent lye.
Description of the drawings
In order to be illustrated more clearly that the specific embodiment of the invention or technical scheme of the prior art, below will be to concrete
Needed for embodiment or description of the prior art, accompanying drawing to be used is briefly described, it should be apparent that, in describing below
Accompanying drawing is some embodiments of the present invention, for those of ordinary skill in the art, before creative work is not paid
Put, can be with according to these other accompanying drawings of accompanying drawings acquisition.
Fig. 1 is the flow chart of industrial alkali waste liquid processing method provided in an embodiment of the present invention；
Fig. 2 is the flow chart of industrial alkali waste liquid treating system provided in an embodiment of the present invention；
Fig. 3 is the pretreatment system flow chart of industrial alkali waste liquid treating system provided in an embodiment of the present invention；
Fig. 4 is the flow chart of the MVR evaporation and crystallization systems of industrial alkali waste liquid treating system provided in an embodiment of the present invention.
Specific embodiment
Technical scheme is clearly and completely described below in conjunction with accompanying drawing, it is clear that described enforcement
Example is a part of embodiment of the invention, rather than the embodiment of whole.Based on the embodiment in the present invention, ordinary skill
The every other embodiment obtained under the premise of creative work is not made by personnel, belongs to the scope of protection of the invention.
In describing the invention, it should be noted that term " " center ", " on ", D score, "left", "right", " vertical ",
The orientation or position relationship of the instruction such as " level ", " interior ", " outward " be based on orientation shown in the drawings or position relationship, merely to
Be easy to description the present invention and simplify description, rather than indicate or imply indication device or element must have specific orientation,
With specific azimuth configuration and operation, therefore it is not considered as limiting the invention.Additionally, term " first ", " second ",
" the 3rd " is 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, meansigma methodss are 5.8 × 104mg/L, account for the 99.99% of total cation, and other cationes
Only<0.01%；
Anion
Anion is with SO4 2-Based on, meansigma methodss are 14.24 × 104mg/L, account for the 99.99% of total anion, and other are cloudy
Ion such as NO2-、NO3-、SO3 2-、S2O3 2-、Cl-Deng only<0.01%；
COD value
COD value changes between 3000-6000ppm.According to theory analysis, by the value for measuring TOC, Organic substance can be calculated
Contribution to COD.In fact, in spent lye, reflect that the COD value of Organic substance only accounts for total COD value about between 30%-40%, and big portion
It is the contribution with reducing substanceses to divide, 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 for surveying2+With Mg2+It is converted into hardness number 21.11-
25.7ppm, difference are larger.Jing after confirming with analysis personnel, learn that total hardness value Jing titrimetry draws, and Ca2+、Mg2+Value is utilized
Spectrographic method draws.Because water quality is complicated, to titrimetry serious interference, affect very big, therefore, total hardness value deviation is larger, therefore with
Ca2+、Mg2+Reflect hardness 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 front road oxidation technology some do not have
It is oxidized completely.To a great extent, it is also one of the reason for improve spent lye COD value.
Turbidity value
Turbidity value>100 degree, this explanation spent lye is muddy, and float and colloid substances are more.
Dissolved oxygen
The excursion of dissolved oxygen value is 4.35-4.5 × 103mg/L, in illustrating Jing 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 to the analysis and research of spent lye water quality data, draw the following conclusions：
Spent lye water-quality constituents is more complicated.But it is main based on sodium sulfate, therefore, reclaim NaSO4 salt and realize resource
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 carry out pretreatment, from effectively process
Technique reduces its COD value and turbidity.
Turbidity value>100, it is necessary to made up to less than 10 before into MVR evaporation and crystallization systems.
Fig. 1 is refer to, the industrial alkali waste liquid processing method that the present invention is provided is comprised the following steps：
Step 1, carries out pretreatment to spent lye, to reduce the COD value and turbidity of spent lye；
Step 1.1, adjusts the Ph values of spent lye；Specifically by the Ph values of spent lye to 3.5；
Step 1.2, the spent lye in feed pump are added to retort by pipe-line mixer with sulphuric acid, while will catalysis
Agent, oxidant also pump into retort, lift response speed, so that mixed liquor stably carries out oxidation reaction under sour environment,
The COD value of spent lye is reduced；
The Ph values of the mixed liquor after oxidation processes are adjusted to 8 by step 1.3；
Step 1.4, using the filler in filter, adsorbs to the COD in mixed liquor, makes the COD of mixed liquor
Below 200ppm is down to, while making turbidity drop to less than 10；
Step 2, is evaporated crystallization using MVR evaporation and crystallization systems to mixed liquor, to separate out sodium sulfate crystal；
Crystal is separated from mixed liquor by step 3 using thickener and seperator, obtains anhydrous sodium sulfate brilliant
Body；Also, the mother solution being centrifuged out is delivered to into MVR evaporation and crystallization systems and continues evaporative crystallization.
The step 2 comprises the steps：
Step 2.1, is preheated to mixed liquor using heat exchanger；
Step 2.2, is evaporated knot using the crystallizing evaporator in MVR evaporation and crystallization systems to pre-warmed mixed liquor
It is brilliant to process；
Step 2.3, is compressed process to the indirect steam that crystallizing evaporator is discharged, and to lift vapor (steam) temperature, then will
Steam is conveyed to the vapour compression machine in MVR evaporation and crystallization systems, to realize recycling for the latent heat of indirect steam, while will
The condensed water that forced circulation heater is discharged is input into into heat exchanger to preheat mixed liquor.
Spent lye in the feed pump passes through line-blending with the sulphuric acid of the regime flow of 8000kg/h and 93% concentration
Device is added to retort.
The industrial alkali waste liquid processing method that the present invention is provided,
Using catalysis oxidation preconditioning technique, impact of the COD value and turbidity in spent lye to subsequent technique is reduced, is improved
The purity of sodium sulfate in spent lye, realizes the recycling of resource.
Using MVR evaporation and crystallization systems (than two-effect evaporation device energy-conservation more than 70%), realize compared with low operating cost.
The water of discharge is made to reach country and cool back target water.
For above-mentioned processing method, Fig. 2-Fig. 4 is refer to, present invention also offers a kind of industrial alkali waste liquid treating system,
The system includes pretreatment system, MVR evaporation and crystallization systems, thickener and the seperator being connected；
Pretreatment system is to reduce in spent lye COD value to below 200ppm, also, the turbidity of spent lye is dropped to 10
Hereinafter, reaching MVR evaporation and crystallization system process demands；
The MVR evaporation and crystallization systems to be evaporated crystallization to the spent lye, to separate out sodium sulfate crystal；
The thickener and seperator obtain anhydrous slufuric acid sodium crystal crystal is separated from mixed liquor；
Also, the mother solution being centrifuged out is delivered to into MVR evaporation and crystallization systems and continues evaporative crystallization.
Refer to the pretreatment system in Fig. 3, this enforcement 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 giving up
Alkali liquor is by pipeline to retort；
The acid solution tank is mixed with spent lye in pipeline acid solution to be delivered to spent lye and be stored by dosing pump, to adjust
The acid-base value of section spent lye is to 3.5；
The catalyst and oxidant tank pass through pipeline communication with retort by dosing pump, to make spent lye with catalysis
Agent and oxidant carry out oxidation reaction under sour environment；
The outlet of the retort passes through dehvery pump and pipe-and-filter is connected, and reduces to the COD value by spent lye
To below 200ppm, turbidity drops to less than 10；
The alkali liquid tank is connected by the pipeline between the outlet of dosing pump and pipeline and retort and dehvery pump, to
The acid-base value of spent lye of retort output is adjusted to 8；The purpose for adjusting acid-base value is allowed for into MVR evaporative crystallization techniques
Needs to Ph values.
The filter is connected with purification water tank by dehvery pump.
Filter adopts filler, and the COD in feed liquid is adsorbed, and reduces about below the COD to 200ppm of spent lye,
Also turbidity is made to drop to less than 10 simultaneously.
Fig. 4 is refer to, the MVR evaporation and crystallization systems in the present embodiment include：Pre-heating system, forced-circulation evaporation system of crystallization
System and steam circulation；
The pre-heating system includes the feed pump being connected and heat exchanger；
The forced-circulation evaporation crystal system includes that forced circulation heater, crystallizing evaporator, mother liquor tank and mother solution are returned
Stream pump；
The forced circulation heater is connected with crystallizing evaporator, and the vaporizer 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 by pipeline and forced circulation heater
Connection, the discharge gate of the heat exchanger are connected with crystallizing evaporator；
The steam circulation includes vapour compression machine and drives the motor of the 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 the first-class heat exchanger being connected and secondary heat exchanger, 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
Before into crystallizing evaporator, its temperature requirement reaches the evaporating temperature of setting to liquid, it is therefore necessary to which feeding liquid is preheated.
In order to make full use of the heat energy of system, by exchanging heat with on-condensible gas heat exchanger, temperature rises to 32 DEG C by 25 DEG C to the spent lye,
Then by exchanging heat with steam condensate (SC) heat exchanger, temperature rises to 88 DEG C by 32 DEG C to spent lye, to reach crystallizing evaporator setting
Temperature.
Preferably,
In view of evaporation efficiency and the factor for preventing calcium ions and magnesium ions easy fouling in evaporation tube, the steaming of vapour compression machine is designed
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, steam
The temperature rise of vapour compressor selects 16 DEG C, there is provided about 7 DEG C or so of effective temperature difference.
Crystallizing evaporator is produced indirect steam and is entered in vapour compression machine by pipeline, and the vapour compression machine is to secondary steaming
Vapour does work so as to temperature lifted to 101 DEG C by 85 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 input into two by pipeline
In level heat exchanger.
As the outlet of vapour compression machine is superheated steam, by compressor outlet spray deionized water, reducing compression
Machine outlet temperature, finally gives saturated vapor.
88 DEG C of spent lye is continuously entered, and oversaturated sodium sulfate 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 granule
Brilliant entrance eluriates lower limb, is detected using densimeter when meeting discharging condition, sequentially enters thickener, centrifuge, and centrifuge is at a high speed
Crystal is separated by rotation, obtains the anhydrous slufuric acid sodium crystal of 5% moisture content；
Centrifuge mother solution out enters mother liquor tank, mother solution is delivered to crystallizing evaporator by pipeline by mother liquor reflux pump
Continue evaporative crystallization.
MVR evaporation and crystallization systems in the industrial alkali waste liquid treating system that the present invention is provided are in evaporation stage system in heat
Poised state, it is not necessary to the extra fresh steam of supplement, heat of the indirect steam that system itself is produced Jing after compressor compression is heated
Enthalpy disclosure satisfy that the heat exchange balance of system feeding, discharging and condensed water etc..
The operating cost of the MVR evaporation and crystallization systems in the present embodiment is than triple effect evaporator energy-conservation 50% or so.The system
The forced-circulation evaporation crystallizer of heat energy recycle and recycled back in system is employed, makes the system that there is preferable energy-conservation
Effect, can not only make cold water recycling water reach national respective standard, and can realize to sodium sulfate crystal in spent lye
Reclaim.
Finally it should be noted that：Various embodiments above only to illustrate technical scheme, rather than a limitation；To the greatest extent
Pipe has been described in detail to the present invention with reference to foregoing embodiments, it will be understood by those within the art that：Its according to
So the technical scheme described in foregoing embodiments can be modified, or which part or all technical characteristic are entered
Row equivalent；And these modifications or replacement, do not make the essence of appropriate technical solution depart from various embodiments of the present invention technology
The scope of scheme.
Claims (10)
1. a kind of industrial alkali waste liquid processing method, it is characterised in that comprise the following steps：
Step 1, carries out pretreatment to spent lye, to reduce the COD value and turbidity of spent lye；
Step 1.1, adjusts the Ph values of spent lye；
Step 1.2, the spent lye in feed pump are added to retort by pipe-line mixer with acid solution, so that mixed liquor is in acid
Property environment under stably carry out oxidation reaction, reduce the COD value of spent lye；
The Ph values of the mixed liquor after oxidation processes are adjusted to 8 by step 1.3；
Step 1.4, using the filler in filter, adsorbs to the COD in mixed liquor, is down to the COD of mixed liquor
Below 200ppm, while making turbidity drop to less than 10；
Step 2, is evaporated crystallization using MVR evaporation and crystallization systems to mixed liquor, to separate out sodium sulfate crystal；
Crystal is separated from mixed liquor by step 3 using thickener and seperator, obtains anhydrous slufuric acid sodium crystal；And
And, the mother solution being centrifuged out is delivered to into MVR evaporation and crystallization systems and continues evaporative crystallization.
2. industrial alkali waste liquid treating system according to claim 1, it is characterised in that the spent lye in the feed pump with
The sulphuric acid of the regime flow of 8000kg/h and 93% concentration is added to retort by pipe-line mixer.
3. industrial alkali waste liquid treating system according to claim 1, it is characterised in that the step 2 comprises the steps：
Step 2.1, is preheated to mixed liquor using heat exchanger；
Step 2.2, is evaporated crystallization to the crystallizing evaporator that pre-warmed mixed liquor is delivered in MVR evaporation and crystallization systems
Process；
Step 2.3, is compressed process to the indirect steam that crystallizing evaporator is discharged, to lift vapor (steam) temperature, then by steam
The vapour compression machine being conveyed in MVR evaporation and crystallization systems, to realize recycling for the latent heat of indirect steam, while will force
The condensed water that recirculation heater is discharged is input into into heat exchanger to preheat mixed liquor.
4. a kind of industrial alkali waste liquid treating system, it is characterised in that including the pretreatment system, MVR evaporative crystallizations system that are connected
System, thickener and seperator；
The pretreatment system is to reduce in spent lye COD value to below 200ppm, also, the turbidity of spent lye is dropped to 10
Hereinafter, reaching MVR evaporation and crystallization system process demands；
The MVR evaporation and crystallization systems to be evaporated crystallization to the spent lye, to separate out sodium sulfate crystal；
The thickener and seperator obtain anhydrous slufuric acid sodium crystal crystal is separated from mixed liquor；Also,
The mother solution being centrifuged out is delivered to into MVR evaporation and crystallization systems and continues evaporative crystallization.
5. industrial alkali waste liquid treating system according to claim 4, 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 is connected by pipeline and spent lye storage pipeline and retort respectively, and the feed pump is to by spent lye
By in pipeline to retort；
The acid solution tank is mixed with spent lye in pipeline acid solution to be delivered to spent lye and be stored by dosing pump, useless to adjust
The acid-base value of alkali liquor；
The catalyst and 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 passes through dehvery pump and pipe-and-filter is connected, the COD value of spent lye to be reduced to
Below 200ppm, turbidity drop to less than 10；
The alkali liquid tank is connected by the pipeline between the outlet of dosing pump and pipeline and retort and dehvery pump, to adjust
The acid-base value of the spent lye of retort output；
The filter is connected with purification water tank by dehvery pump.
6. industrial alkali waste liquid treating system according to claim 4, it is characterised in that the MVR evaporation and crystallization systems bag
Include：Pre-heating system, forced-circulation evaporation crystal system and steam circulation；
The pre-heating system includes the feed pump being connected and heat exchanger；
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 vaporizer discharging opening is connected with thickener, the stiff
Device discharging opening is connected with seperator；
The mother liquor reflux pump intake is connected with seperator, and mother liquor reflux pump discharge is connected with forced circulation heater by pipeline
Logical, the discharge gate of the heat exchanger is connected with crystallizing evaporator；
The steam circulation includes vapour compression machine and drives the motor of the vapour compression machine；
The vapour compression machine is connected with crystallizing evaporator and forced circulation heater respectively.
7. industrial alkali waste liquid treating system according to claim 4, it is characterised in that the heat exchanger includes what is be connected
First-class 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.
8. industrial alkali waste liquid treating system according to claim 7, it is characterised in that
By exchanging heat with on-condensible gas heat exchanger, temperature rises to 32 DEG C by 25 DEG C to the spent lye, then spent lye by with steaming
Vapour condensation water- to-water heat exchanger heat exchange, temperature rises to 88 DEG C by 32 DEG C, to reach the temperature of crystallizing evaporator setting.
9. industrial alkali waste liquid treating system according to claim 8, it is characterised in that crystallizing evaporator produces indirect steam
By pipeline enter vapour compression machine in, the vapour compression machine to indirect steam do work so as to temperature by 85 DEG C lifted to
101 DEG C, then circulation conveying, finally make secondary to forced circulation heater to realize recycling for the latent heat of indirect steam
Steam condensation becomes 101 DEG C of condensed water, and condensed water is input into into secondary heat exchanger by pipeline.
10. industrial alkali waste liquid treating system according to claim 9, it is characterised in that 88 DEG C of spent lye is continuously entered
Flash distillation is carried out in crystallizing evaporator, oversaturated sodium sulfate is precipitated in crystallizing evaporator, the heavy of crystallization is precipitated by control
Drop time and path, make crystal grow in crystallizing evaporator, and the larger crystallization of granule is entered eluriates lower limb, is detected using densimeter
When discharging condition is met, thickener, centrifuge are sequentially entered, separated by rotation at a high speed by crystal for centrifuge, is obtained 5% and is contained
The anhydrous slufuric acid sodium crystal of water rate；
Centrifuge mother solution out enters mother liquor tank, mother solution is delivered to crystallizing evaporator continuation by pipeline by mother liquor reflux pump
Evaporative crystallization.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611194122.4A CN106587477A (en) | 2016-12-21 | 2016-12-21 | System and method for treating industrial waste lye |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611194122.4A CN106587477A (en) | 2016-12-21 | 2016-12-21 | System and method for treating industrial waste lye |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106587477A true CN106587477A (en) | 2017-04-26 |
Family
ID=58600447
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611194122.4A Pending CN106587477A (en) | 2016-12-21 | 2016-12-21 | System and method for treating industrial waste lye |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106587477A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107867709A (en) * | 2017-12-11 | 2018-04-03 | 广州叶林环保科技有限公司 | A kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization |
| CN108275821A (en) * | 2018-03-15 | 2018-07-13 | 北京燕山翔宇环保工程技术有限公司 | A kind of desulfurization wastewater treatment system and its treatment process |
| CN109481952A (en) * | 2018-11-28 | 2019-03-19 | 江苏瑞升华能源科技有限公司 | A kind of MVR crystallizes out salt crystal grain control system and control method |
| CN110372052A (en) * | 2019-07-09 | 2019-10-25 | 中国航发哈尔滨东安发动机有限公司 | A kind of isolated island formula miniature gas turbine vapor recompression system and control method |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5783084A (en) * | 1997-05-01 | 1998-07-21 | Suenkonis; Charles M. | Process for the reclamation of process water from process wastewater generated in the battery manufacturing industry and other metals related industries |
| JP2011020074A (en) * | 2009-07-17 | 2011-02-03 | Sasakura Engineering Co Ltd | Apparatus and method for solidifying solution or liquid waste |
| CN102530997A (en) * | 2012-02-28 | 2012-07-04 | 信义电子玻璃（芜湖）有限公司 | Desulfurization product recycling technology and system |
| CN102815812A (en) * | 2011-06-10 | 2012-12-12 | 中国石油化工股份有限公司 | Optimization process method for recovering sodium sulfate form ethylene waste alkali |
| CN104326612A (en) * | 2014-10-24 | 2015-02-04 | 南京科盛环保科技有限公司 | Method and system for recovering salt from waste water treatment system |
| CN204873906U (en) * | 2015-08-27 | 2015-12-16 | 北京浦仁美华节能环保科技有限公司 | Anti - technology evaporation crystallization device that circulates |
| CN105836951A (en) * | 2016-05-23 | 2016-08-10 | 江苏瑞升华能源科技有限公司 | Treatment process and device of electroplating wastewater |
| CN205473138U (en) * | 2016-01-11 | 2016-08-17 | 中国石油化工股份有限公司 | Comprehensive processing apparatus of alkaline residue waste liquid |
| CN206444229U (en) * | 2016-12-21 | 2017-08-29 | 北京燕山翔宇环保工程技术有限公司 | MVR evaporation and crystallization systems and industrial alkali waste liquid treating system |
-
2016
- 2016-12-21 CN CN201611194122.4A patent/CN106587477A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5783084A (en) * | 1997-05-01 | 1998-07-21 | Suenkonis; Charles M. | Process for the reclamation of process water from process wastewater generated in the battery manufacturing industry and other metals related industries |
| JP2011020074A (en) * | 2009-07-17 | 2011-02-03 | Sasakura Engineering Co Ltd | Apparatus and method for solidifying solution or liquid waste |
| CN102815812A (en) * | 2011-06-10 | 2012-12-12 | 中国石油化工股份有限公司 | Optimization process method for recovering sodium sulfate form ethylene waste alkali |
| CN102530997A (en) * | 2012-02-28 | 2012-07-04 | 信义电子玻璃（芜湖）有限公司 | Desulfurization product recycling technology and system |
| CN104326612A (en) * | 2014-10-24 | 2015-02-04 | 南京科盛环保科技有限公司 | Method and system for recovering salt from waste water treatment system |
| CN204873906U (en) * | 2015-08-27 | 2015-12-16 | 北京浦仁美华节能环保科技有限公司 | Anti - technology evaporation crystallization device that circulates |
| CN205473138U (en) * | 2016-01-11 | 2016-08-17 | 中国石油化工股份有限公司 | Comprehensive processing apparatus of alkaline residue waste liquid |
| CN105836951A (en) * | 2016-05-23 | 2016-08-10 | 江苏瑞升华能源科技有限公司 | Treatment process and device of electroplating wastewater |
| CN206444229U (en) * | 2016-12-21 | 2017-08-29 | 北京燕山翔宇环保工程技术有限公司 | MVR evaporation and crystallization systems and industrial alkali waste liquid treating system |
Non-Patent Citations (1)
| Title |
|---|
| 上海市经济团体联合会等: "《节能减排工程技术与应用案例》", vol. 1, 华东理工大学出版社, pages: 262 - 264 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107867709A (en) * | 2017-12-11 | 2018-04-03 | 广州叶林环保科技有限公司 | A kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization |
| CN108275821A (en) * | 2018-03-15 | 2018-07-13 | 北京燕山翔宇环保工程技术有限公司 | A kind of desulfurization wastewater treatment system and its treatment process |
| CN109481952A (en) * | 2018-11-28 | 2019-03-19 | 江苏瑞升华能源科技有限公司 | A kind of MVR crystallizes out salt crystal grain control system and control method |
| CN110372052A (en) * | 2019-07-09 | 2019-10-25 | 中国航发哈尔滨东安发动机有限公司 | A kind of isolated island formula miniature gas turbine vapor recompression system and control method |
| CN110372052B (en) * | 2019-07-09 | 2021-09-24 | 中国航发哈尔滨东安发动机有限公司 | Island type micro gas turbine steam recompression system and control method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105585194B (en) | One kind contains Na+、K+、NH4+、Cl‑、SO42‑、NO3‑The highly concentrated effluent brine method of comprehensive utilization of coal chemical industry | |
| CN104326612B (en) | A kind of method and system reclaiming salt from Waste Water Treatment | |
| CN109292797A (en) | A kind of brine waste sub-prime recovery method | |
| CN108358369A (en) | A kind of brine waste is concentrated by evaporation mother liquor and divides salt treatment process method and device | |
| CN103553138B (en) | Comprehensive utilization method for separating, concentrating and purifying manganese sulfate, magnesium sulfate and calcium sulfate in high-salt waste water | |
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| CN105523676B (en) | A kind of high-salinity wastewater zero-emission crystalline salt by evaporation sub-prime method | |
| CN104973726A (en) | Recovery processing method of high salinity wastewater containing sodium chloride and sodium sulfate | |
| CN106587477A (en) | System and method for treating industrial waste lye | |
| CN105314783A (en) | Coal-fired power plant desulfurization waste water zero-emission treating technology and device special for treating technology | |
| CN206444229U (en) | MVR evaporation and crystallization systems and industrial alkali waste liquid treating system | |
| CN113105138A (en) | Method and system for water washing dechlorination of waste incineration fly ash and evaporation mass-separation crystallization of water washing liquid | |
| CN209367818U (en) | A kind of brine waste sub-prime recovery system | |
| CN108558098A (en) | A kind of method for treating desulfurized wastewater and device | |
| CN108101290A (en) | A kind of electroplating waste-water reutilizing and the processing system and processing method of zero-emission | |
| CN106115740B (en) | A kind of salt extraction process and salt making system | |
| CN205241427U (en) | Desulfurization wastewater treatment system | |
| CN110615456A (en) | Device and process for continuously producing aluminum sulfate octadecahydrate | |
| CN105523677A (en) | Treatment system capable of realizing zero discharge of desulfurization wastewater | |
| CN114195316A (en) | Iron phosphate wastewater treatment system and treatment method | |
| CN111573942A (en) | Method for recycling copper-nickel electroplating waste liquid | |
| CN207862094U (en) | A kind of electroplating waste-water reutilizing and the processing system of zero-emission | |
| CN205347092U (en) | Desulfurization waste water zero release processing system | |
| CN105481160B (en) | Method and device for preparing industrial salt by strong brine with zero discharge | |
| CN105152186A (en) | Technique for simple substance salt separation with co-production of sodium sulfide from high-salinity wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |