CN110255692A - In a kind of photovoltaic industry concentrated acid wastewater by sequencing batch formula and accurate control method - Google Patents
In a kind of photovoltaic industry concentrated acid wastewater by sequencing batch formula and accurate control method Download PDFInfo
- Publication number
- CN110255692A CN110255692A CN201910604001.XA CN201910604001A CN110255692A CN 110255692 A CN110255692 A CN 110255692A CN 201910604001 A CN201910604001 A CN 201910604001A CN 110255692 A CN110255692 A CN 110255692A
- Authority
- CN
- China
- Prior art keywords
- waste water
- formula
- control method
- photovoltaic industry
- concentrated acid
- 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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
-
- 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
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/583—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing fluoride or fluorine compounds
-
- 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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
Abstract
The invention discloses in a kind of batch-type of photovoltaic industry concentrated acid waste water and accurate control method, belong to field of waste water treatment.The following steps are included: being followed the steps below as pH≤3 in waste water: a) adding CaCO into waste water3Neutralization reaction is carried out as medicament is neutralized, the pH value of waste water is adjusted to 3 < pH≤7；B) Ca (OH) is added first into step 1) treated waste water2, then add CaCl2Carry out neutralization reaction；As 3 < pH≤7 in waste water, Ca (OH) is directly added into waste water2And CaCl2, neutralize and fluorine removal reacted.The present invention provides a kind of neutralization control method for regulating and controlling the batch-type of adding of agent, small water according to the pH value of waste water, the problem of overcoming in the prior art in the treatment process of photovoltaic industry concentrated acid waste water since acid-base neutralization reaction is violent, medicament package caused to cause reaction efficiency low and be easy to damage equipment due to exothermic effect.
Description
Technical field
The present invention relates to a kind of control methods for the concentrated acid waste liquid neutralisation treatment that photovoltaic industry generates, and belong to wastewater treatment neck
Domain.
Background technique
The photovoltaic energy is green energy resource, but the production of especially photovoltaic cell is deposited in photovoltaic industry production process
In more serious pollution, wherein the discharge of water pollutant is very important, environmental issue be photovoltaic industry develop maximum restriction because
Element.Photovoltaic industry is divided into upstream, midstream and downstream according to production product difference, and upstream industry mainly produces monocrystalline silicon and polysilicon
Silicon wafer, middle reaches industry mainly utilize mono-/multi- crystalline silicon wafer to produce solar battery, and downstream industry mainly produces photovoltaic generating system
And other products.The discharge of wastewater of photovoltaic industry is concentrated mainly on upstream and midstream, generates during manufacture of solar cells
A large amount of concentrated acid waste liquid.
It is mainly HF, HNO in the concentrated acid waste liquid that photovoltaic industry generates3、HCl、H2SO4, waste water is highly acid, and pH value is general
In 1mol/L or more or 0~4 range, and HF acid has strong oxidizing property, strong corrosive, and harm is larger, the wastewater treatment
It is difficult.For such concentrated acid waste liquid that photovoltaic industry generates, due to the radius very little of the fluorine ion in hydrofluoric acid, this causes
It has very strong permeability, and corrosivity is extremely strong, is to be most difficult to corrosion-resistant substance.According to titanium or graphite material its higher cost,
Therefore existing treatment process is still based on neutralizing.
Existing treatment process mainly utilizes Ca (OH)2、CaCl2Sour neutralization, fluorine removal are carried out, by multi stage precipitation and is filtered off
Except the calcium fluoride precipitate in waste water, is mixed again with other waste water after being disposed and carry out biochemical treatment.Such as number of patent application
CN201710172660.1, publication date are that the application case on June 20th, 2017 discloses a kind of photovoltaic industry sewage classification processing
Method, specific steps are as follows: categorised collection is carried out to sewage using different pipelines in the sewage collecting stage, sewage is divided into organic
Waste water, particle waste water, high conductance waste water and acid-bearing wastewater；Organic wastewater is handled using MBR technique, reaches its water outlet
Reuse standard；Particle waste water is handled using the method that filters pressing and sand filtration combine, its water outlet is made to reach reuse standard；It adopts
High conductance waste water is handled with double film extracting and concentrating technologies, its water outlet is made to reach reuse standard；Using white lime combination precipitator
Skill handles acid-bearing wastewater, its water outlet is made to reach discharge standard.
However, existing treatment process mainly has following drawback: (1) added amount of chemical is excessive and medicament kind is single.
During underway and reaction, due to being strong acid and concentration height in acid solution, so in acid-base neutralization on medicament surface
Vigorous reaction occurs, medicament is caused to wrap up, internal medicament cannot participate in reacting, thus cause added amount of chemical excessive, resource
Waste.The medicament complexity of enterprise in order to reduce operation during adding is not recycled sufficiently using single dosage component simultaneously
Valuable element causes the medicament wasting of resources.(2) dosage for neutralizing medicament can not be precisely controlled.In the prior art, neutralizating medicine
The variation that the dosage of agent mainly passes through pH value in reactor is adjusted, and is not to be calculated according to the concentration of fluorine ion,
And adding of agent may be caused excessive in reactor due to the monitoring hysteresis quality of pH value on-line detector, it can not be precisely controlled.
(3) acutely, heat release is serious for reaction.Since neutralization reaction is a kind of exothermic reaction, play can be occurred by adding medicament when acid stronger
A large amount of heat is released in strong reaction, and cold and hot frequent switching causes equipment, pipeline easy to damage, and operational safety is poor, while can also make
It is serious at sour gas volatilization.(4) impact resistance is small.The stage of photovoltaic industry concentrated acid waste water generation, water have biggish
Fluctuation, since the volume of single-reactor is larger, the size for causing the dosage of medicament to be difficult the water of basis is changed tune
Section causes to neutralize adding of agent excess or deficiency.
Therefore the defect based on the prior art, needs to invent a kind of neutralization control method that reaction efficiency is high.
Summary of the invention
1. to solve the problems, such as
For, since acid-base neutralization reaction is violent, leading to medicine in the treatment process of photovoltaic industry concentrated acid waste water in the prior art
The problem of agent wraps up and is acutely easy to damage equipment due to exothermic effect, the present invention provide a kind of according to the pH value of waste water regulation medicine
The neutralization control method of batch-type, small water that agent adds.
2. technical solution
To solve the above-mentioned problems, the technical solution adopted in the present invention is as follows:
The present invention provides in a kind of batch-type of photovoltaic industry concentrated acid waste water and accurate control method, specifically:
It as pH≤3 in waste water, follows the steps below: a) adding CaCO into waste water3It is carried out as medicament is neutralized
The pH value of waste water is adjusted to 3 < pH≤7 by neutralization reaction；B) Ca (OH) is added first into step 1) treated waste water2, then
Add CaCl2Carry out neutralization reaction；
As 3 < pH≤7 in waste water, Ca (OH) is directly added into waste water2And CaCl2, neutralize and fluorine removal reacted.
As further improvement of the present invention, as pH≤3 in waste water, the step a) is specific as follows:
If 1) H in waste water+Concentration >=1mol/L adds CaCO to waste water for M1 according to dosage3, the M1 is according to public affairs
Formula 1 calculates:
M1=60* (CH +- 1) formula 1；
In formula, M1 unit is kg/m3；CH +For H in waste water+Molar concentration, mol/L；By pH value of waste water tune in the step
It saves to 0 < pH≤3；
2) if pH value of waste water is 0 < pH≤3；CaCO is added to waste water according to dosage for M23, the M2 is according to formula 2
It calculates:
M2=60* (10-pH- 0.001) formula 2；
In formula, M2 unit is kg/m3；PH is pH reading, dimensionless in waste water.
As further improvement of the present invention, in the step b), follow the steps below:
It is M according to dosageCa(OH)2Ca (OH) is added first2, it is M according still further to dosageCaCl2Add CaCl2, described
MCa(OH)2It is calculated according to formula 3, the MCaCl2It is calculated according to formula 4:
MCa(OH)2=45*10-pHFormula 3；
MCaCl2=3*CF-- M1-M2 formula 4；
In formula, pH is pH reading, dimensionless in waste water；MCa(OH)2Unit is kg/m3；MCaCl2Unit is kg/m3；CF-It is useless
F in water-Concentration, g/L, M1 are CaCO in step 1)3Dosage, unit kg/m3；M2 is CaCO in step 2)3Add
Amount, unit kg/m3；If calculating MCaCl2Dosage is less than 0, then it represents that no longer adds, if not being related to M1 in step, recognizes
For M1=0.
It is the M according to dosage as 3 < pH≤7 in waste water as further improvement of the present inventionCa(OH)2It is first
First add Ca (OH)2, CaCl is added according still further to 3 times of amount of fluorinion in waste water concentration2。
As further improvement of the present invention, generated in use aqueous slkali collection reaction process in the step 1)
CO2, then carry out recycling reuse.
As further improvement of the present invention, the device that neutralization reaction is carried out in the step 1) and step 2) is tank
Body, the volume of the tank body are Q0m3/ h, the unlatching of the tank body is according to waste water water Q and Q0Comparison calculated, work as waste water
Water Q≤Q0When, open a neutralization reaction device；As waste water water Q > Q0When, need to open n tank body；As waste water water Q
It is Q0Integer multiple when, n=Q/Q0；As the non-Q of waste water water Q0Integer multiple when, n=Q/Q0+1。
As further improvement of the present invention, the Q0Value be 1~5m3/h。
As further improvement of the present invention, heat-exchange device is set on the tank body, absorbs neutralization reaction release
Heat, damage caused by preventing gradient of temperature from causing the expansion of equipment and pipeline and shrinking.
As further improvement of the present invention, the heat-exchange device uses coil heat exchanger.
3. beneficial effect
Compared with the prior art, the invention has the benefit that
(1) in photovoltaic industry concentrated acid wastewater by sequencing batch formula of the invention and accurate control method, according to H in waste water+Concentration becomes
Change the type of adjustment adding of agent, the H in waste water+When concentration is relatively high, it is firstly added CaCO3It is neutralized, generates carbon dioxide
It is received using lye and recycles corresponding carbonate, reuse can be carried out to save operating cost, neutralization is adjusted to 3 < pH≤7 in waste water
When, using being firstly added Ca (OH)2, add CaCl2Mode carry out neutralize and fluorine removal, on the one hand effectively prevent Ca (OH)2
The problem for causing pH ascensional range excessively high excessively is added, the halfway disadvantage of fluorine removal caused by the other hand preventing because of dosage deficiency
End.The invention patent makes full use of medicament feature itself, controls adding of agent type and dosage, overcomes prior art Chinese medicine
Add unreasonable, the biggish defect of dosage.
(2) dense according to hydrogen ion in waste water in photovoltaic industry concentrated acid wastewater by sequencing batch formula of the invention and accurate control method
Successively decreasing for degree is precisely controlled the dosage of medicament, avoids adding of agent excessive.On the other hand, using the dosing method energy of batch-type
The phenomenon that once largely adding caused medicament package in the prior art is enough effectively reduced and reduced, the reaction effect of medicament is enhanced
Efficiency and utilization rate are answered, to reduce added amount of chemical.
(3) in photovoltaic industry concentrated acid wastewater by sequencing batch formula of the invention and accurate control method, reaction heat can quickly be recycled
Amount controls reactor temperature climbing speed, is specifically reacted using small water, and coil pipe heat exchange is arranged on reacting tank body
Device can control neutralization reaction and remain within the scope of a steady temperature, prevent quickly by the heat absorption of neutralization reaction
Only equipment eventually leads to equipment damage because of gradient of temperature generation temperature deformation.Meanwhile the heat that exchanger absorbs is for plant area
Heating unit utilizes, it can be achieved that resource makes full use of, and then realizes the production energy-saving of photovoltaic industry.
(4) in photovoltaic industry concentrated acid wastewater by sequencing batch formula of the invention and accurate control method, entire reaction, chemicals dosing plant can
Test Automatic Control.The control program of dosing type and dosage is set in neutralization reaction, while certainly according to water fluctuation
The dynamic tank body that adjusts opens quantity, can be completely achieved the Automatic Control of reaction, and total system is realized online linkage and control, is not necessarily to
Manual operation.
(5) in photovoltaic industry concentrated acid wastewater by sequencing batch formula of the invention and accurate control method, have to water fluctuation very strong
Resiliency.The present invention controls opening for reacting tank body by water compared with the volume size of neutralization reaction tank body, adjustment
The number of reacting tank body is participated in, and then optimizes the parameter of neutralization reaction, while guaranteeing reaction effect, is had to water fluctuation
Very strong cushion performance.
(6) in photovoltaic industry concentrated acid wastewater by sequencing batch formula of the invention and accurate control method, carbanion can be recycled,
Utilizing CaCO3A large amount of carbon dioxide gas can be generated during neutralization, received during gas collection using NaOH
Generation soda ash can be reacted, soda ash can be recycled in on-site, make full use of medicament resource, can also use Ca (OH)2It connects
It receives, generates CaCO3, then neutralize strongly acid wastewater.
Detailed description of the invention
Fig. 1 is the process flow chart in embodiment 4.
Specific embodiment
The present invention is further described below combined with specific embodiments below.
Embodiment 1
Photovoltaic industry highly acid waste liquid 1L is taken, HF content is 30% in waste water, fluorinion concentration 15g/L, HNO3Contain
Amount is 10%, and in addition there are a small amount of HCl and H2SO4, H through detecting, in waste water+Concentration is about 18mol/L, and pH is far longer than
1mol/L。
As H in waste water+When concentration is greater than 1mol/L, according to formula M1=60* (CH +- 1) it calculates, obtains CaCO3Add
The absolute magnitude of amount is 1020g/L, i.e. kg/m3, the CaCO for being 40% with mass concentration during adding3The form of slurries adds,
It is stirred during adding, residence time 2h, pH is 0.5 after fully reacting；
As 0 < pH of waste water≤3, according to formula M2=60* (10-pH- 0.001) it calculates, obtains CaCO3Dosage it is exhausted
It is 18.91g/L, i.e. kg/m to amount3, the CaCO for being 40% with mass concentration during adding3The form of slurries adds, and is throwing
It is stirred during adding, residence time 1h, pH is 3.2 after fully reacting；
As 3 < pH of waste water≤7, according to formula MCa(OH)2=45*10-pH, MCaCl2=3*CF-- M1-M2 is computed, Ca
(OH)2The absolute magnitude of dosage is 0.028g/L, i.e. kg/m3, CaCl2It is calculated as negative value, expression does not need to add.Ca(OH)2?
It adds, is stirred during adding, residence time 0.5h in the form of mass concentration is 40% slurries during adding, reacted
PH is 7 or more after completely.
Entire neutralization and fluorine removal process are completed after three phases.
The H in waste water+When concentration is greater than 1mol/L and 0 < pH≤3, the CO generated in reaction process is collected2, CO2Gas is adopted
It is received with NaOH solution, then carries out resource utilization.
During the three phases of reaction, the sediment of generation is collected, main component CaF2, can be returned
It receives and utilizes.
Embodiment 2
Taking photovoltaic industry acid pickle 1L, acid pickle pH is 1.5, and the main component of spent acid is HF, HNO3, HCl and H2SO4Deng,
Wherein the concentration of fluorine ion is 8g/L.
Firstly, when 0 < pH of waste water≤3, according to formula M2=60* (10-Ph- 0.001) it calculates, obtains CaCO3Dosage
Absolute magnitude be 1.84g/L, during adding by mass concentration be 40% slurries in the form of add, stirred during adding
It mixes, residence time 1h, pH is 3.0 after fully reacting；
Then, according to the calculation formula M of 3 < pH≤7Ca(OH)2=45*10-pH, MCaCl2=3*CF-- M1-M2, wherein M1=0,
M2=1.84g/L is computed, Ca (OH)2Adding absolute magnitude is 0.045g/L, CaCl2The absolute magnitude of dosage is 22.16g/L.
Ca(OH)2It is added in the form of mass concentration is 40% slurries during adding, CaCl2With mass concentration during adding
Form for 50% slurries adds, and stirs during adding, and residence time 1h, pH is 7 or more after fully reacting.
Embodiment 3
Taking photovoltaic industry acid pickle 1L, acid pickle pH is 4, and the main component of spent acid is HF, HNO3, HCl and H2SO4Deng,
The concentration of middle fluorine ion is 0.6g/L.
According to the calculation formula M of 3 < pH≤7Ca(OH)2=45*10-pH, MCaCl2=3*CF-- M1-M2 is computed, Ca (OH)2
Adding absolute magnitude is 0.005g/L, CaCl2The absolute magnitude of dosage is 1.8g/L.Ca(OH)2With mass concentration during adding
Form for 40% slurries adds, CaCl2It adds, was adding in the form of mass concentration is 50% slurries during adding
It is stirred in journey, residence time 1h, pH is 7 or more after fully reacting.
Embodiment 4
As shown, carrying out pilot experiment in the sewage treatment region of photovoltaic industry, acid pickle is strongly acid wastewater, waste water
Middle HF content is 30%, HNO3Content be 10%, in addition there are a small amount of HCl and H2SO4.H through detecting, in waste water+Concentration
About 18mol/L, fluorinion concentration 15g/L.
Pilot experiment water Q=2m3/ h, the volume of single neutralization reaction tank body are Q0=2m3/h.According to Q=Q0, therefore
Only open a neutralization reaction tank body.Coil heat exchanger is set in neutralization reaction tank interior surrounding, medium is cold in coil pipe
Salt water absorbs the heat of neutralization reaction release, prevents that temperature rapid increase.
A) as H in waste water+When concentration is greater than 1mol/L, CaCO is automatically turned on3The valve of adding of agent.According to formula M1=
60*(CH +- 1) it calculates, obtains CaCO3Dosage absolute magnitude be 1020kg/m3, with the shape of 50% slurries during adding
Formula adds, and stirs during adding, and residence time 5h, pH rises to 0.1 after fully reacting；
B) after pH rises to 0 or more, according to pH on-line computing model data, CaCO is continued starting3The valve of adding of agent, is pressed
According to formula M2=60* (10-pH- 0.001) it calculates, obtains CaCO3Dosage absolute magnitude be 47.66kg/m3, adding process
In added in the form of 50% slurries, stirred during adding, residence time 3h, pH rises to 3.0 after fully reacting；
C) it after pH rises to 3 or more, according to pH on-line computing model data, opens Ca (OH)2And CaCl2The valve of adding of agent
Door, according to formula MCa(OH)2=45*10-pH, MCaCl2=3*CF-- M1-M2 is computed, Ca (OH)2The absolute magnitude of dosage is
0.045kg/m3, CaCl2It does not need to add.Ca(OH)2It is added in the form of mass concentration is 40% slurries during adding,
It is stirred during adding, residence time 0.5h, pH is 7 or more after fully reacting.
Embodiment 5
Carry out pilot experiment, carries out pilot experiment in the sewage treatment region of photovoltaic industry, acid pickle pH is 1.5, spent acid
Main component be HF, HNO3, HCl and H2SO4Deng, wherein the concentration of fluorine ion be 8g/L.
Pilot experiment water Q=6m3/ h, the volume that single neutralization reaction tank body is arranged is Q0=3m3/h.It is Q according to Q0's
Integer multiple, n=Q/Q0=2, therefore open 2 neutralization reaction tank bodies.The surrounding setting coil pipe heat outside neutralization reaction tank body
Exchanger, medium is cool brine in coil pipe, absorbs the heat of neutralization reaction release, prevents that temperature rapid increase.
A) according to pH on-line computing model data, when 0 < pH of waste water≤3, CaCO is automatically turned on3The valve of adding of agent.According to
Formula M2=60* (10-Ph- 0.001) it calculates, obtains CaCO3Dosage absolute magnitude be 1.84kg/m3, during adding
It adds, is stirred during adding, residence time 2h, pH exists after fully reacting in the form of mass concentration is 40% slurries
3.3；
B) it after pH rises to 3 or more, according to pH on-line computing model data, automatically turns on Ca (OH)2And CaCl2Adding of agent
Valve, according to formula MCa(OH)2=45*10-pH, MCaCl2=3*CF-- M1-M2 is computed, Ca (OH)2Adding absolute magnitude is
0.023kg/m3, CaCl2The absolute magnitude of dosage is 22.16kg/m3。Ca(OH)2During adding in the form of 40% slurries
It adds, CaCl2It is added in the form of 50% slurries during adding, is stirred during adding, residence time 1h, reaction
PH is 7 or more after completely.
Embodiment 6
Carry out production run in the sewage treatment region of photovoltaic industry, acid pickle pH is 4, the main component of spent acid be HF,
HNO3, HCl and H2SO4Deng, wherein the concentration of fluorine ion be 0.6g/L.
Water Q=12m3/ h, the volume that single neutralization reaction tank body is arranged is Q0=5m3/h.It is Q according to Q0Non-integer
Multiple, n=Q/Q0+ 1=3, therefore open 3 neutralization reaction tank bodies.It is handed in neutralization reaction tank interior surrounding setting coil pipe heat
Parallel operation, medium is cool brine in coil pipe, absorbs the heat of neutralization reaction release, prevents that temperature rapid increase.
According to pH on-line computing model data, waste liquid 3 < pH≤7 are automatically turned on Ca (OH)2And CaCl2The valve of adding of agent,
According to formula MCa(OH)2=45*10-pH, MCaCl2=3*CF-, it is computed Ca (OH)2Adding absolute magnitude is 0.005kg/m3, CaCl2It throws
The absolute magnitude of dosage is 1.8kg/m3。Ca(OH)2It is added in the form of 40% slurries during adding, CaCl2Adding process
In added in the form of 50% slurries, stirred during adding, residence time 1h, pH is 7 or more after fully reacting.Reaction
Entire neutralization and fluorine removal process are completed after completely.
Claims (9)
1. in a kind of photovoltaic industry concentrated acid wastewater by sequencing batch formula and accurate control method, it is characterised in that: follow the steps below:
It as pH≤3 in waste water, follows the steps below: a) adding CaCO into waste water3Neutralize instead as medicament is neutralized
It answers, the pH value of waste water is adjusted to 3 < pH≤7；B) Ca (OH) is added first into step 1) treated waste water2, then add
CaCl2Carry out neutralization reaction；
As 3 < pH≤7 in waste water, Ca (OH) is directly added into waste water2And CaCl2, neutralize and fluorine removal reacted.
2. in photovoltaic industry concentrated acid wastewater by sequencing batch formula according to claim 1 and accurate control method, it is characterised in that:
As pH≤3 in waste water, the step a) is specific as follows:
If 1) H in waste water+Concentration >=1mol/L adds CaCO to waste water for M1 according to dosage3, the M1 is according to the meter of formula 1
It calculates:
M1=60* (CH +- 1) formula 1；
In formula, M1 unit is kg/m3；CH +For H in waste water+Molar concentration, mol/L；PH value of waste water is adjusted to 0 in the step <
pH≤3；
2) if pH value of waste water is 0 < pH≤3；CaCO is added to waste water according to dosage for M23, the M2 is according to the calculating of formula 2:
M2=60* (10-pH- 0.001) formula 2；
In formula, M2 unit is kg/m3；PH is pH reading, dimensionless in waste water.
3. in photovoltaic industry concentrated acid wastewater by sequencing batch formula according to claim 2 and accurate control method, it is characterised in that: institute
It states in step b), follows the steps below:
It is M according to dosageCa(OH)2Ca (OH) is added first2, it is M according still further to dosageCaCl2Add CaCl2, the MCa(OH)2It presses
It is calculated according to formula 3, the MCaCl2It is calculated according to formula 4:
MCa(OH)2=45*10-pHFormula 3；
MCaCl2=3*CF-- M1-M2 formula 4；
In formula, pH is pH reading, dimensionless in waste water；MCa(OH)2Unit is kg/m3；MCaCl2Unit is kg/m3；CF-For in waste water
F-Concentration, g/L, M1 are CaCO in step 1)3Dosage, unit kg/m3；M2 is CaCO in step 2)3Dosage, it is single
Position is kg/m3；If calculating MCaCl2Dosage is less than 0, then it represents that no longer adds.
4. in photovoltaic industry concentrated acid wastewater by sequencing batch formula according to claim 3 and accurate control method, it is characterised in that:
It is M according to dosage as 3 < pH≤7 in waste waterCa(OH)2Ca (OH) is added first2, according still further to fluorinion in waste water concentration
3 times of amount adds CaCl2。
5. existing in the batch-type of photovoltaic industry concentrated acid waste water according to claim 1 or 2 with accurate control method, feature
In: the CO generated in reaction process is collected in the step 1) using aqueous slkali2, then carry out recycling reuse.
6. in photovoltaic industry concentrated acid wastewater by sequencing batch formula according to claim 5 and accurate control method, it is characterised in that: institute
Stating and carrying out the device of neutralization reaction in step 1) and step 2) is tank body, and the volume of the tank body is Q0m3/ h, the tank body are opened
It opens according to waste water water Q and Q0Comparison calculated, as waste water water Q≤Q0When, open a neutralization reaction device；When useless
Water water Q > Q0When, need to open n tank body；When waste water water Q is Q0Integer multiple when, n=Q/Q0；When waste water water Q is non-
Q0Integer multiple when, n=Q/Q0+1。
7. in photovoltaic industry concentrated acid wastewater by sequencing batch formula according to claim 6 and accurate control method, it is characterised in that: institute
State Q0Value be 1~5m3/h。
8. in photovoltaic industry concentrated acid wastewater by sequencing batch formula according to claim 7 and accurate control method, it is characterised in that: institute
It states and heat-exchange device is set on tank body, absorb the heat of neutralization reaction release, prevent gradient of temperature from causing the swollen of equipment and pipeline
Damage caused by swollen and contraction.
9. in photovoltaic industry concentrated acid wastewater by sequencing batch formula according to claim 8 and accurate control method, it is characterised in that:,
The heat-exchange device uses coil heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910604001.XA CN110255692A (en) | 2019-07-05 | 2019-07-05 | In a kind of photovoltaic industry concentrated acid wastewater by sequencing batch formula and accurate control method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910604001.XA CN110255692A (en) | 2019-07-05 | 2019-07-05 | In a kind of photovoltaic industry concentrated acid wastewater by sequencing batch formula and accurate control method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110255692A true CN110255692A (en) | 2019-09-20 |
Family
ID=67924650
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910604001.XA Pending CN110255692A (en) | 2019-07-05 | 2019-07-05 | In a kind of photovoltaic industry concentrated acid wastewater by sequencing batch formula and accurate control method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110255692A (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1351968A (en) * | 2001-12-20 | 2002-06-05 | 南化集团研究院 | Treating method for high fluorice acid waste water |
| CN103373776A (en) * | 2012-04-17 | 2013-10-30 | 上海晶宇环境工程有限公司 | Up-to-standard discharging process for fluoride-containing wastewater generated by photovoltaic industry and dedicated system of up-to-standard discharging process |
| CN104326602A (en) * | 2014-11-11 | 2015-02-04 | 湖北理工学院 | Method and device for sequencing batch treatment of fluorine/nickel-containing acidic wastewater in aluminum profile production |
| CN105347574A (en) * | 2015-12-10 | 2016-02-24 | 浙江奇彩环境科技有限公司 | Fluoride removal method of graphite purification waste water and processing system |
| CN205892984U (en) * | 2016-06-17 | 2017-01-18 | 云南今业生态建设集团有限公司 | Production life effluent disposal system of photovoltaic energy enterprise |
| CN106745626A (en) * | 2016-12-01 | 2017-05-31 | 郑州亦森环保科技有限公司 | The processing method of fluoride waste and application |
| CN108689522A (en) * | 2018-05-24 | 2018-10-23 | 江苏南大环保科技有限公司 | A kind of Treatment and recovery recovery method of photovoltaic industry nitration mixture waste water |
| CN109020019A (en) * | 2018-10-30 | 2018-12-18 | 湖北凯乐量子通信光电科技有限公司 | A kind of acidic fluorine-containing waste water purifying processing device |
-
2019
- 2019-07-05 CN CN201910604001.XA patent/CN110255692A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1351968A (en) * | 2001-12-20 | 2002-06-05 | 南化集团研究院 | Treating method for high fluorice acid waste water |
| CN103373776A (en) * | 2012-04-17 | 2013-10-30 | 上海晶宇环境工程有限公司 | Up-to-standard discharging process for fluoride-containing wastewater generated by photovoltaic industry and dedicated system of up-to-standard discharging process |
| CN104326602A (en) * | 2014-11-11 | 2015-02-04 | 湖北理工学院 | Method and device for sequencing batch treatment of fluorine/nickel-containing acidic wastewater in aluminum profile production |
| CN105347574A (en) * | 2015-12-10 | 2016-02-24 | 浙江奇彩环境科技有限公司 | Fluoride removal method of graphite purification waste water and processing system |
| CN205892984U (en) * | 2016-06-17 | 2017-01-18 | 云南今业生态建设集团有限公司 | Production life effluent disposal system of photovoltaic energy enterprise |
| CN106745626A (en) * | 2016-12-01 | 2017-05-31 | 郑州亦森环保科技有限公司 | The processing method of fluoride waste and application |
| CN108689522A (en) * | 2018-05-24 | 2018-10-23 | 江苏南大环保科技有限公司 | A kind of Treatment and recovery recovery method of photovoltaic industry nitration mixture waste water |
| CN109020019A (en) * | 2018-10-30 | 2018-12-18 | 湖北凯乐量子通信光电科技有限公司 | A kind of acidic fluorine-containing waste water purifying processing device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| TWI353875B (en) | Removing carbon dioxide from waste streams through | |
| CN103011453B (en) | Processing method for fluoride waste water in production of solar cells | |
| CN102259838B (en) | Method for continuously preparing hydrogen fluoride by using rotary reaction furnace | |
| JP6071892B2 (en) | Perfluoride decomposition treatment method and treatment apparatus | |
| CN100509658C (en) | High-concentration chromium-containing wastewater resource treatment method | |
| CN102502880B (en) | Utilize the method that acid-washing waste acid produces iron series water purifier | |
| CN204918124U (en) | Fenton oxidation degradation waste water COD's reaction unit | |
| CN105251231B (en) | The exhaust treatment system and method for organic silicon low-boiling-point substance conversion reaction | |
| CN206318826U (en) | Desulfurization wastewater treatment system and automatic waste water processing system | |
| CN103613146B (en) | The method for innocent treatment of iron protochloride | |
| CN110255692A (en) | In a kind of photovoltaic industry concentrated acid wastewater by sequencing batch formula and accurate control method | |
| CN206089294U (en) | Steel industry hydrochloric acid pickling liquid waste's processing recovery system | |
| CN112813443A (en) | Pickling solution iron removal regeneration equipment and method | |
| CN102660751A (en) | Resourceful treating method and resourceful treating device for metal pickling effluent | |
| CN110255823A (en) | A kind of high zinc high ammonia nitrogen and high thiocarbamide waste water treatment process | |
| CN109945711A (en) | A kind of exothermic method and apparatus of chemical heat accumulation- | |
| CN208087250U (en) | The device that high-salt wastewater low-temperature evaporation is concentrated using hot industry waste water | |
| CN104548636B (en) | Concentration and evaporation device in zirconium oxychloride production technology | |
| CN202347032U (en) | Chrome tanning agent production unit | |
| CN103183430A (en) | Device for treating ammonia nitrogen wastewater by utilizing direct contact type degassing membrane technology | |
| CN104524797B (en) | Energy-conservation concentration and evaporation method in zirconium oxychloride production process | |
| CN102732650B (en) | Production process and dedicated production equipment for chrome tanning agent | |
| CN207671862U (en) | One kind being used for coal chemical industry enterprises high-concentration ammonia nitrogenous wastewater recycling treatment system | |
| CN105439108A (en) | Method and device for resource recycling of silicon core corrosion waste liquor | |
| CN215946982U (en) | Comprehensive treatment system for waste gas of thermal power plant |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190920 |
|
| RJ01 | Rejection of invention patent application after publication |