CN106219643A - A kind of concentration cycles utilizes the method for industry high-salt wastewater - Google Patents
A kind of concentration cycles utilizes the method for industry high-salt wastewater Download PDFInfo
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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
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
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- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/33—Wastewater or sewage treatment systems using renewable energies using wind energy
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
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- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The present invention relates to field of industrial waste water treatment, in particular it relates to a kind of method that concentration cycles utilizes industry high-salt wastewater.The concentration cycles of the present invention utilizes the method for industry high-salt wastewater, comprises the following steps: 1) by industry high-salt wastewater natural evaporation, until carrying out solid-liquid separation after separating out solid phase, it is thus achieved that sodium chloride and the first evaporation mother solution；2) by step 1) the evaporation mother solution that obtains carries out freezing processing, under field conditions (factors) until carrying out solid-liquid separation after having solid separation, it is thus achieved that Natrii Sulfas and freezing mother solution；3) by step 2) the freezing mother solution that obtains carries out natural evaporation, until carrying out solid-liquid separation after having solid separation, it is thus achieved that the salt-mixture of sodium chloride and Natrii Sulfas and the second evaporation mother solution.Present invention process is simple, it is easy to operation, and process conditions are gentle；There is no complex device construction, reduce input cost；Being more suitable for processing on a large scale high-salt wastewater, the scale of construction is the biggest, and efficiency is the highest.
Description
Technical field
The present invention relates to field of industrial waste water treatment, in particular it relates to a kind of concentration cycles utilizes industry high salt
The method of waste water.
Background technology
In Chinese society economic development and urbanization process, it is sustainable that water scarcity is being increasingly becoming restriction China
One of principal element of development strategy.In recent years, along with China's commercial scale constantly increases, industrial water consumption increases sharply；But, produce
Raw wastewater flow rate increases the most rapidly, processes to current waste water and brings huge challenge with recovery and utilization technology.Industrial wastewater is as directly
Discharge, will produce serious pollution to surrounding soil, water body environment；Waste water treated qualified up to standard after, if do not recycled, then
Cause water resource waste, aggravate shortage of water resources.
Dense salt waste water mostlys come from the strong brine in circulation concentrated solution, demineralized water preparation process, and produces
The strong brine produced during sanitary wastewater process and regeneration and the various medicaments of interpolation.
For high-salt wastewater, owing to lacking feasibility technically, economically and reliability, great majority are taked to dilute outer row
Method.This method not only can not really reduce the total emission volumn of pollutant, and causes the waste of fresh water；Particularly saliferous gives up
The discharge of water, certainly will cause freshwater resources mineralising and alkalization of soils.With external high-salt wastewater " zero-emission " or " become zero-emission "
Desalting technology level is compared, and there is bigger gap in China.Therefore, how exploiting economy effective high-salt wastewater desalting processing technique skill
Art, promotes the recycling of high-salt wastewater, is to solve the bottleneck problem that water resource recycles.
Processing method currently mainly has:
1. bioanalysis
Utilize salt-durable microbe and halophilic microorganism to process brine waste, there is certain range of application.
2. electrochemical process
The method of electrochemical oxidation degradable organic pollutant mainly has 2 kinds: Electrocatalytic Oxidation method and Indirect Electrooxidation.Before
Person is that the free radical (such as hydroxyl radical free radical) utilizing electrode surface to produce carrys out oxidative degradation Organic substance；The latter is the oxidation to generate
Agent (such as hypochlorous acid) carrys out oxidative degradation Organic substance.
3. ion-exchange process
Ion exchange is a unit process, in this process, generally involves the ion in solution with insoluble
Property polymer (containing fixing anion or cation) on counter ion between exchange reaction.Use ion exchange desalination
Time, waste water first passes around cation exchange column, the most positively charged ion (Na+Deng) by H+Replace and be trapped in exchange column；
Afterwards, electronegative ion (Cl-Deng) in anion-exchange column by OH-Displacement, reaches the purpose of desalination.
4. membrane separation process
Membrane separation technique is to utilize film that diactinic difference of compositional selecting each in mixture is separated, purifies and concentrated
The new separation technology of target substance.
5. heating evaporation technique
Heating evaporation technique is one of modern chemical industry means of cell operation, i.e. by the method for heating, makes the part in solution
Solvent evaporation is also removed, and to improve the concentration of solution, or creates conditions for solute precipitation.
Above-mentioned each existing processing method all there are disadvantages that, specific as follows:
1. bioanalysis shortcoming
Inorganic salt in high saliferous industrial wastewater has stronger inhibitory action to microorganism, for the growing environment of microorganism
Causing the biggest puzzlement, screening and cultivation domestication difficulty simultaneously for related microorganisms are high, and the body of industry high-salt wastewater
Measuring huge, therefore the popularization and application for bioanalysis have the biggest restriction.
2. electrochemical process shortcoming
Electrochemical process is higher to the conduction needs of high-salt wastewater, due to the complicated component of high-salt wastewater, for electrode
To compare strict, i.e. investment is big, and cost is high；Additionally energy-output ratio is big, and electrode material consumes too much, when reactant concentration is the highest
Time process time lengthening, current efficiency reduce.
3. ion-exchange process shortcoming
One subject matter of this method is that the solid suspension in waste water can block resin and lose effect, is exactly also ion
The regeneration of exchanger resin needs high expense and the very difficult process of refuse exchanged.
4. membrane separation process shortcoming
The most conventional membrane technology has ultrafiltration, microfiltration, electrodialysis and reverse osmosis.Ultrafiltration therein, microfiltration give up for high salt
During the process of water, it is impossible to effectively remove the salinity in sewage；Electrodialysis and reverse osmosis technical finesse cost height, operating experience are not
Foot, reverse osmosis technology application in terms of municipal sewage treatment and Industrial Wastewater Treatment receives a definite limitation.Membrane technology method
If shortcoming is organic concentration height in waste water, film is easily contaminated, thus causes operating process to be difficult to run well, moreover tonne
It is high that waste water carries out film processing cost, and enterprise is difficult to bear.
5. heating evaporation processing disadvantages
Heating evaporation needs multi-effect evaporator, though it is more in chemical industry application, but the case that brine waste is processed
Less, do not have the successful experience can for reference, and the water quality of each enterprise brine waste differs greatly, evaporation process effect and handling
With the most different.Separately because of particularity and the complexity of composition of waste water itself, the quality of the salt steamed needs to be verified.This method is transported
Costly, energy resource consumption is big, also can bring secondary pollution for row.
Although additionally, prior art also having some use the method concentration Industry Waste that evaporation combines with freezing
Water, but these methods are required to rely on particular instrument to carry out, complex process, and input cost is too high, and, the equal nothing of these methods
The process waste water of the big scale of construction of method.
Summary of the invention
It is an object of the invention to, for the shortcoming of prior art, it is provided that a kind of efficient concentration recycles industry high salt and gives up
The method of water
The concentration cycles of the present invention utilizes the method for industry high-salt wastewater, comprises the following steps:
1) by industry high-salt wastewater natural evaporation, it is more than until separating out sulfate ion mass concentration in solid phase and liquid phase
Solid-liquid separation is carried out, it is thus achieved that sodium chloride and the first evaporation mother solution after 2.0%；
2) by step 1) the evaporation mother solution that obtains carries out freezing processing, under field conditions (factors) until having solid separation and liquid phase
Middle sulfate ion mass concentration carries out solid-liquid separation after being less than or equal to 1.0%, it is thus achieved that Natrii Sulfas and freezing mother solution；
3) by step 2) the freezing mother solution that obtains carries out natural evaporation, until there being sulfate ion in solid separation and liquid phase
Mass concentration carries out solid-liquid separation after should be greater than equal to 1.8%, it is thus achieved that sodium chloride is female with the salt-mixture of Natrii Sulfas and the second evaporation
Liquid.
The waste water that industry high-salt wastewater of the present invention produces mainly for ore dressing, chemical enterprise, leading ion and dense
Degree scope Na+: 5～50g/L, Cl-: 5～50g/L, SO4 2-: 5～50g/L；Salinity is at the waste water of more than 60g/L.
The method according to the invention, wherein, preferably by step 3) the second evaporation mother solution and step 1 of obtaining) obtain the
After one evaporation mother solution mixing, repeat step 2) with 3), it is circulated and concentrates until total metal concentration symbol in last evaporation mother solution
Close demand of industrial production.Further, the volume ratio of described second evaporation mother solution and the first evaporation mother solution is 1:10～1:50.
According to method of the present invention, wherein, step 3) obtain second evaporation mother solution in heavy metal ion relative
After industry high-salt wastewater is concentrated 10～200 times, makes the second evaporation mother solution enter heavy metal ion and extract workshop, reclaim profit
With.
Heavy metal of the present invention is i.e. heavy metal well known in the art, refers generally to density and is more than 5, and major part is at periodic chart
In belong to transition element metal and ion thereof, such as cadmium (Cd), hydrargyrum (Hg), lead (Pb), arsenic (As), copper (Cu), zinc (Zn), chromium
(Cr), nickel (Ni) etc..
Method in accordance with the invention it is preferred that step 2) temperature of described freezing is-1～-20 DEG C, cooling time be 5～
20 days.
Further, refrigerating process and evaporation process order can also be exchanged by the present invention, to reach identical mesh
Mark.Scheme after order is exchanged is as follows:
Concentration cycles of the present invention utilizes the method for industry high-salt wastewater, comprises the following steps:
1) industry high-salt wastewater is carried out under field conditions (factors) freezing processing, until there being sulfate radical in solid separation and liquid phase
Mass of ion concentration carries out solid-liquid separation after being less than or equal to 1.0%, it is thus achieved that ice and freezing mother solution；
2) by step 1) the freezing mother solution that obtains carries out natural evaporation, until separating out sulfate ion matter in solid phase and liquid phase
Amount concentration carries out solid-liquid separation after being more than or equal to 2.0%；Obtain sodium chloride and the first evaporation mother solution；
3) by step 2) obtain first evaporation mother solution carry out natural evaporation, until there being sulfate radical in solid separation and liquid phase
Mass of ion concentration carries out solid-liquid separation after should be greater than equal to 1.8%, it is thus achieved that sodium chloride steams with the salt-mixture and second of Natrii Sulfas
Send out mother solution.
The method according to the invention, freezing is formerly evaporated in posterior scheme, it is preferable that by step 3) the second steaming of obtaining
Send out mother solution and step 1) after the freezing mother solution that obtains mix, repeat step 2) and 3), it is circulated concentration until last evaporation
In mother solution, total metal concentration meets demand of industrial production.Further, described second evaporation mother solution and the mass ratio of freezing mother solution
For 1:10～1:50.
The method according to the invention, freezing is formerly evaporated in posterior scheme, it is preferable that step 3) the second evaporation of obtaining
After heavy metal ion in mother solution is concentrated 10～200 times relative to industry high-salt wastewater, the second evaporation mother solution is made to enter a huge sum of money
Belong to the ion extraction workshop, recycle.
The method according to the invention, freezing is formerly evaporated in posterior scheme, it is preferable that step 1) temperature of described freezing
For-1～-20 DEG C, cooling time is 5～20 days.
Advantages of the present invention is as follows:
1, green energy conservation, environmental friendliness, there is no energy resource consumption, it is to avoid secondary pollution；
2, make full use of the solar energy in nature, wind energy, cold energy, reduce into product cost；
3, technique is simple, it is easy to operation, and process conditions are gentle；
4, there is no complex device construction, reduce input cost；
5, being more suitable for processing high-salt wastewater on a large scale, the scale of construction is the biggest, and efficiency is the highest.
Accompanying drawing explanation
Fig. 1 is the process schematic representation (first freezing after evaporation) of the concentration cycles utilization industry high-salt wastewater of the present invention.
Fig. 2 is the process schematic representation (evaporating after first freezing) of the concentration cycles utilization industry high-salt wastewater of the present invention.
Fig. 3 is 25 DEG C of Na+/Cl-,SO4 2--H2O ternary system metastable phase diagram (evaporation process first).
Fig. 4 is-5 DEG C of Na+/Cl-,SO4 2--H2O ternary system metastable phase diagram (freezing processing procedure).
Fig. 5 is 25 DEG C of Na+/Cl-,SO4 2--H2O ternary system metastable phase diagram (evaporation process again).
Detailed description of the invention
The present invention is expanded on further by the following examples, and these embodiments are only used for the purpose illustrated, not
Limit the scope of the present invention.The test method of unreceipted actual conditions in the following example, generally according to normal condition.
Embodiment 1
The leading ion of the industrial high-salt wastewater studied and concentration range Na+: 5～50g/L, Cl-: 5～50g/L,
SO4 2-: 5～50g/L, remaining be heavy metal such as cadmium (Cd), hydrargyrum (Hg), lead (Pb), arsenic (As), copper (Cu), zinc (Zn), chromium (Cr),
Nickel (Ni) etc.；Salinity is at more than 60g/L；Its pH value is between 8～12, aobvious alkaline.
Evaporation-freezing-evaporation technology
First the industrial high-salt wastewater obtained is carried out filtering and impurity removing, then this high-salt wastewater is at room temperature evaporated (about
20 DEG C), to solid separation, when sulfate radical mass content is more than 2.5% in liquid phase, carries out solid-liquid separation, obtain solid phase 1 and mother solution 1
(the first evaporation mother solution) separates out solid phase 1 predominantly sodium chloride.
The mother solution 1 removing sodium chloride is carried out freezing processing, when temperature is at-3.9 DEG C, solution begins with solid phase analysis
Go out, predominantly Natrii Sulfas (sal glauberi), when sulfate radical mass content is less than 1.0% in liquid phase, Natrii Sulfas is divided again with mother solution 1
From, it is thus achieved that Natrii Sulfas by-product and mother solution 2 (freezing mother solution), mother solution 2 is carried out room temprature evaporation (about 20 DEG C), removes a part of water
After, have solid separation, in liquid phase sulfate radical mass content more than 2.0% time obtain sodium chloride and Natrii Sulfas salt-mixture and mother solution 3 (the
Two evaporation mother solutions), then mother solution 3 and mother solution 1 are converted halogen, and (mother solution 3 is 1:20 with the mass ratio of mother solution 1, and circulation carries out above-mentioned work
Process flow.
Finally, until process cycles several times after, in mother solution 3, associated metal content reaches requirement (heavy metal ion is relative to work
Industry high-salt wastewater is concentrated 10～200 times) after, enter relevant workshop and carry out extracting separation.
Step (1): gathered industry high-salt wastewater system point at figure 3 above (25 DEG C of Na+//Cl-,SO4 2--H2O ternary system
Metastable phase diagram) at C point, this high-salt wastewater is evaporated, be evaporated to D point, now, system be divided into A (solid phase 1: sodium sulfate) and
E1(mother solution 1) two parts；Mother solution is carried out freezing process, is illustrated in fig. 4 shown below:
At-5 DEG C of Na+//Cl-,SO4 2--H2On O ternary system metastable phase diagram it can be seen that carry out freezing after, it is possible to obtain
S10(solid phase 2) and E2(mother solution 2)；By E2(mother solution 2) again in room temperature evaporate, evaporation process as shown in Figure 5:
By E2(mother solution 2) is evaporated to G point, and now G point is made up of B (NaCl) and mother solution 3, carries out solid-liquid separation, it is thus achieved that
NaCl product, then carries out recycling by mother solution 3.
No waste discharge during whole, operation stream becomes simple, it is achieved that the repetition of resource, recycle, circulation technology
Green, friendly.
Embodiment 2
The leading ion of the industrial high-salt wastewater studied and concentration range Na+: 5～50g/L, Cl-: 5～50g/L,
SO4 2-: 5～50g/L, remaining be heavy metal such as cadmium (Cd), hydrargyrum (Hg), lead (Pb), arsenic (As), copper (Cu), zinc (Zn), chromium (Cr),
Nickel (Ni) etc.；Salinity is at more than 60g/L；Its pH value is between 8～12, aobvious alkaline.
Freezing-evaporation-evaporation technology
First the industrial high-salt wastewater obtained is carried out filtering and impurity removing, then by this high-salt wastewater at cold energy (about-8 DEG C) bar
Process under part, to solid separation, when sulfate radical mass content is close to 1.5% in liquid phase, carry out solid-liquid separation, obtain solid phase 1 and mother
Liquid 1 (the first evaporation mother solution) separates out solid phase 1 (predominantly ice).
It is evaporated processing (about 20 DEG C) by the mother solution 1 removing ice, when solution has solid separation, predominantly sodium chloride,
In liquid phase, sulfate radical mass content is close to 2.5%, solid sodium chloride is again separated with mother solution 1, it is thus achieved that sodium chloride byproduct and
Mother solution 2 (freezing mother solution), carries out mother solution 2 natural evaporation (about 25 DEG C), after removing a part of water, has solid phase 3 to separate out, predominantly
Sodium chloride and Natrii Sulfas, when sulfate radical mass content≤1.0% in liquid phase, separate, it is thus achieved that mother solution 3 (the second evaporation mother solution)
With solid phase 3, then mother solution 3 and mother solution 1 being converted halogen (mother solution 3 is 1:20 with the mass ratio of mother solution 1), circulation carries out above-mentioned technique stream
Journey.
Finally, until process cycles several times after, in mother solution 3 heavy metals content relative to industry high-salt wastewater be concentrated 10
～after 200 times, enter relevant workshop and carry out extracting separation.
No waste discharge during whole, operation stream becomes simple, it is achieved that the repetition of resource, recycle, circulation technology
Green, friendly.
Embodiment 3
The leading ion of the industrial high-salt wastewater studied and concentration range Na+: 5～50g/L, Cl-: 5～50g/L,
SO4 2-: 5～50g/L, remaining be heavy metal such as cadmium (Cd), hydrargyrum (Hg), lead (Pb), arsenic (As), copper (Cu), zinc (Zn), chromium (Cr),
Nickel (Ni) etc.；Salinity is at more than 60g/L；Its pH value is between 8～12, aobvious alkaline.
Evaporation-freezing-evaporation technology
First the industrial high-salt wastewater obtained is carried out filtering and impurity removing, then this high-salt wastewater is at room temperature evaporated (about
20 DEG C), to solid separation, when sulfate radical mass content is close to 2.0% in liquid phase, carry out solid-liquid separation, obtain solid phase 1 and mother solution 1
(the first evaporation mother solution) separates out solid phase 1 predominantly sodium chloride.
The mother solution 1 removing sodium chloride is carried out freezing processing, when temperature is at-1 DEG C, solution begins with solid separation,
Predominantly Natrii Sulfas (sal glauberi), when in liquid phase, sulfate radical mass content is close to 1.0%, separates with mother solution 1 again by Natrii Sulfas,
Obtain Natrii Sulfas by-product and mother solution 2 (freezing mother solution), mother solution 2 is carried out room temprature evaporation (about 20 DEG C), after removing a part of water, has
Solid separation, in liquid phase, sulfate radical mass content is close to obtaining sodium chloride and Natrii Sulfas salt-mixture and mother solution 3 (the second steaming when 1.8%
Send out mother solution), then mother solution 3 and mother solution 1 are converted halogen, and (mother solution 3 is 1:10 with the mass ratio of mother solution 1, and circulation carries out above-mentioned technique stream
Journey.
Finally, until process cycles several times after, in mother solution 3, associated metal content reaches requirement (heavy metal ion is relative to work
Industry high-salt wastewater is concentrated 10～200 times) after, enter relevant workshop and carry out extracting separation.
No waste discharge during whole, operation stream becomes simple, it is achieved that the repetition of resource, recycle, circulation technology
Green, friendly.
Embodiment 4
The leading ion of the industrial high-salt wastewater studied and concentration range Na+: 5～50g/L, Cl-: 5～50g/L,
SO4 2-: 5～50g/L, remaining be heavy metal such as cadmium (Cd), hydrargyrum (Hg), lead (Pb), arsenic (As), copper (Cu), zinc (Zn), chromium (Cr),
Nickel (Ni) etc.；Salinity is at more than 60g/L；Its pH value is between 8～12, aobvious alkaline.
Freezing-evaporation-evaporation technology
First the industrial high-salt wastewater obtained is carried out filtering and impurity removing, then by this high-salt wastewater at cold energy (about-20 DEG C)
Under the conditions of process, to solid separation, when sulfate radical mass content is close to 1.0% in liquid phase, carry out solid-liquid separation, obtain solid phase 1 He
Mother solution 1 (the first evaporation mother solution) separates out solid phase 1 (predominantly ice).
It is evaporated processing (about 20 DEG C) by the mother solution 1 removing ice, when solution has solid separation, predominantly sodium chloride,
When solid phase there being sodium sulfate separate out (sulfate radical mass content close to 2.0%), solid sodium chloride is separated again with mother solution 1,
Obtain sodium chloride byproduct and mother solution 2 (freezing mother solution), mother solution 2 is carried out natural evaporation (about 25 DEG C), after removing a part of water,
There is solid phase 3 to separate out, predominantly sodium chloride and Natrii Sulfas, when sulfate radical mass content is close to 1.8%, separate, it is thus achieved that mother solution 3
(the second evaporation mother solution) and solid phase 3, then convert halogen (mother solution 3 is 1:50 with the mass ratio of mother solution 1), circulation by mother solution 3 and mother solution 1
Carry out above-mentioned technological process.
Finally, until process cycles several times after, in mother solution 3 heavy metals content relative to industry high-salt wastewater be concentrated 10
～after 200 times, enter relevant workshop and carry out extracting separation.
No waste discharge during whole, operation stream becomes simple, it is achieved that the repetition of resource, recycle, circulation technology
Green, friendly.
Certainly, the present invention can also have various embodiments, in the case of without departing substantially from present invention spirit and essence thereof, is familiar with
Those skilled in the art can make various corresponding change and deformation according to disclosure of the invention, but these change accordingly and
Deformation all should belong to the scope of the claims of the present invention.
Claims (10)
1. the method that concentration cycles utilizes industry high-salt wastewater, comprises the following steps:
1) by industry high-salt wastewater natural evaporation, it is not less than until separating out sulfate ion mass concentration in solid phase and liquid phase
Solid-liquid separation is carried out, it is thus achieved that sodium chloride and the first evaporation mother solution after 2.0%；
2) by step 1) the evaporation mother solution that obtains carries out freezing processing, under field conditions (factors) until there being sulfur in solid separation and liquid phase
Acid ion mass concentration carries out solid-liquid separation after being less than or equal to 1.0%, it is thus achieved that Natrii Sulfas and freezing mother solution；
3) by step 2) the freezing mother solution that obtains carries out natural evaporation, until there being sulfate ion quality in solid separation and liquid phase
Concentration carries out solid-liquid separation after being less than or equal to 1.0%, it is thus achieved that sodium chloride evaporates mother solution with the salt-mixture and second of Natrii Sulfas.
Method the most according to claim 1, it is characterised in that by step 3) obtain second evaporation mother solution and step 1) obtain
After the first evaporation mother solution mixing obtained, repeat step 2) and 3).
Method the most according to claim 2, it is characterised in that described second evaporation mother solution and the quality of the first evaporation mother solution
Ratio is 1:10～1:50.
4. according to the arbitrary described method of claim 1-3, it is characterised in that step 3) weight in the second evaporation mother solution of obtaining
After metal ion is concentrated 10～200 times relative to industry high-salt wastewater, makes the second evaporation mother solution enter heavy metal ion and extract
Workshop, recycles.
5. according to the arbitrary described method of claim 1-4, it is characterised in that step 2) temperature of described freezing is-1～-20
DEG C, cooling time is 5～20 days.
6. the method that concentration cycles utilizes industry high-salt wastewater, comprises the following steps:
1) industry high-salt wastewater is carried out under field conditions (factors) freezing processing, until there being sulfate ion in solid separation and liquid phase
Mass concentration carries out solid-liquid separation after being less than or equal to 1.0%, it is thus achieved that ice and freezing mother solution；
2) by step 1) the freezing mother solution that obtains carries out natural evaporation, until it is dense to separate out sulfate ion quality in solid phase and liquid phase
Degree carries out solid-liquid separation after being more than or equal to 2.0%；Obtain sodium chloride and the first evaporation mother solution；
3) by step 2) obtain first evaporation mother solution carry out natural evaporation, until there being sulfate ion in solid separation and liquid phase
Mass concentration carries out solid-liquid separation after should be greater than equal to 1.8%, it is thus achieved that sodium chloride is female with the salt-mixture of Natrii Sulfas and the second evaporation
Liquid.
Method the most according to claim 6, it is characterised in that by step 3) obtain second evaporation mother solution and step 1) obtain
After the freezing mother solution mixing obtained, repeat step 2) and 3).
Method the most according to claim 7, it is characterised in that described second evaporation mother solution with the mass ratio of freezing mother solution is
1:10～1:50.
9. according to the arbitrary described method of claim 6-8, it is characterised in that step 3) weight in the second evaporation mother solution of obtaining
After metal ion is concentrated 10～200 times relative to industry high-salt wastewater, makes the second evaporation mother solution enter heavy metal ion and extract
Workshop, recycles.
10. according to the arbitrary described method of claim 6-9, it is characterised in that step 1) temperature of described freezing is-1～-20
DEG C, cooling time is 5～20 days.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109437442A (en) * | 2018-12-25 | 2019-03-08 | 苏州清然环保科技有限公司 | The analysis salt device and analysis salt method of high-salt wastewater |
| CN109607654A (en) * | 2019-01-31 | 2019-04-12 | 内蒙古科技大学 | Device, method and the application of strong brine low temperature crystallization desalination |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102009041456A1 (en) * | 2009-09-12 | 2011-03-24 | K-Utec Ag Salt Technologies | Producing high percentage potassium chloride from polymineralic, magnesium sulfate rich crude potassium salt or from crude salt fraction obtained during dry treatment of crude salt, comprises hot dissolution-cold crystallization process |
| CN102336421A (en) * | 2011-07-27 | 2012-02-01 | 陈海通 | Double-salt field method for preparing sodium sulfate based on mother liquid treatment |
| CN103204512A (en) * | 2012-10-18 | 2013-07-17 | 中国科学院青海盐湖研究所 | Method for preparing boron rock from plateau sulfate type salt lake brine |
| 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 |
| CN104609633A (en) * | 2015-02-16 | 2015-05-13 | 阮氏化工（常熟）有限公司 | Method and device for utilizing sewage containing ammonia and sodium |
| CN105084651A (en) * | 2015-07-28 | 2015-11-25 | 山西诺凯化工技术有限公司 | Purification treatment and pure-salt recovery process for strong-salt wastewater in coal chemical industry |
| CN105110542A (en) * | 2015-09-14 | 2015-12-02 | 济宁璟华环保科技有限公司 | Zero-discharge salt separation and purification method for industrial high-salt wastewater |
| CN105384293A (en) * | 2015-11-16 | 2016-03-09 | 河北钢铁股份有限公司承德分公司 | Treatment method for vanadium precipitation wastewater subjected to impurity removal and deamination |
-
2016
- 2016-07-22 CN CN201610583595.7A patent/CN106219643A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102009041456A1 (en) * | 2009-09-12 | 2011-03-24 | K-Utec Ag Salt Technologies | Producing high percentage potassium chloride from polymineralic, magnesium sulfate rich crude potassium salt or from crude salt fraction obtained during dry treatment of crude salt, comprises hot dissolution-cold crystallization process |
| CN102336421A (en) * | 2011-07-27 | 2012-02-01 | 陈海通 | Double-salt field method for preparing sodium sulfate based on mother liquid treatment |
| CN103204512A (en) * | 2012-10-18 | 2013-07-17 | 中国科学院青海盐湖研究所 | Method for preparing boron rock from plateau sulfate type salt lake brine |
| 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 |
| CN104609633A (en) * | 2015-02-16 | 2015-05-13 | 阮氏化工（常熟）有限公司 | Method and device for utilizing sewage containing ammonia and sodium |
| CN105084651A (en) * | 2015-07-28 | 2015-11-25 | 山西诺凯化工技术有限公司 | Purification treatment and pure-salt recovery process for strong-salt wastewater in coal chemical industry |
| CN105110542A (en) * | 2015-09-14 | 2015-12-02 | 济宁璟华环保科技有限公司 | Zero-discharge salt separation and purification method for industrial high-salt wastewater |
| CN105384293A (en) * | 2015-11-16 | 2016-03-09 | 河北钢铁股份有限公司承德分公司 | Treatment method for vanadium precipitation wastewater subjected to impurity removal and deamination |
Non-Patent Citations (1)
| Title |
|---|
| 田立楠等: "《盐化工概论》", 30 June 1992, 华中理工大学出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109437442A (en) * | 2018-12-25 | 2019-03-08 | 苏州清然环保科技有限公司 | The analysis salt device and analysis salt method of high-salt wastewater |
| CN109607654A (en) * | 2019-01-31 | 2019-04-12 | 内蒙古科技大学 | Device, method and the application of strong brine low temperature crystallization desalination |
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