CN106757258B - Oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saver and technique - Google Patents
Oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saver and technique Download PDFInfo
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- CN106757258B CN106757258B CN201611043945.7A CN201611043945A CN106757258B CN 106757258 B CN106757258 B CN 106757258B CN 201611043945 A CN201611043945 A CN 201611043945A CN 106757258 B CN106757258 B CN 106757258B
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25D—PROCESSES FOR THE ELECTROLYTIC OR ELECTROPHORETIC PRODUCTION OF COATINGS; ELECTROFORMING; APPARATUS THEREFOR
- C25D11/00—Electrolytic coating by surface reaction, i.e. forming conversion layers
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- C25D11/00—Electrolytic coating by surface reaction, i.e. forming conversion layers
- C25D11/02—Anodisation
- C25D11/04—Anodisation of aluminium or alloys based thereon
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25D—PROCESSES FOR THE ELECTROLYTIC OR ELECTROPHORETIC PRODUCTION OF COATINGS; ELECTROFORMING; APPARATUS THEREFOR
- C25D11/00—Electrolytic coating by surface reaction, i.e. forming conversion layers
- C25D11/02—Anodisation
- C25D11/04—Anodisation of aluminium or alloys based thereon
- C25D11/06—Anodisation of aluminium or alloys based thereon characterised by the electrolytes used
- C25D11/08—Anodisation of aluminium or alloys based thereon characterised by the electrolytes used containing inorganic acids
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- C25D11/00—Electrolytic coating by surface reaction, i.e. forming conversion layers
- C25D11/02—Anodisation
- C25D11/04—Anodisation of aluminium or alloys based thereon
- C25D11/06—Anodisation of aluminium or alloys based thereon characterised by the electrolytes used
- C25D11/10—Anodisation of aluminium or alloys based thereon characterised by the electrolytes used containing organic acids
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- C25D21/00—Processes for servicing or operating cells for electrolytic coating
- C25D21/02—Heating or cooling
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- C25D21/00—Processes for servicing or operating cells for electrolytic coating
- C25D21/16—Regeneration of process solutions
- C25D21/18—Regeneration of process solutions of electrolytes
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Abstract
Oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saver and technique, technique include oxidation solution circulating cooling step, aluminium ion crystalline product recycling step, sulfuric acid oxidation liquid recycling step, gas agitating step and defrosting step；The aluminium ion crystalline product recycling step includes: that oxidation solution is imported reactor tank, and ammonium aluminum sulfate crystal is precipitated after ammonium sulfate is added into reactor tank, then the material in reactor tank is imported in centrifuge to the solid and liquid being centrifuged after being separated by solid-liquid separation；The sulfuric acid oxidation liquid recycling step includes: the oxidation solution collected after crystallization treatment, is delivered to anodizing tank recycling after carrying out regeneration treatment to oxidation solution.The present invention proposes oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saver and technique, by extracting the aluminium in oxidation solution, recycles sulfuric acid, reduce oxidation solution resistance, corrosion inhibiter is added in oxidation solution, reduces the meltage of oxidation film to realize oxidation energy conservation, 20% or more energy conservation.
Description
Technical field
The present invention relates to the technical field of aluminum product processing more particularly to oxidation trough aluminium ion and retrieval of sulfuric acid and oxidations
Liquid inhibition energy saver and technique.
Background technique
Aluminium alloy forms the oxidation film characterized by porosity after anodized, in aluminium material surface, it is necessary to pass through
Sealing pores are obtained with physical and chemical performances such as the corrosion resistances, weatherability and wearability that guarantee aluminium alloy anode oxide product
Durable service performance.
Building alumilite process liquid refers to tank liquor used in aluminium alloy anode oxide.When fluting, anodizing solution H2SO4It is dense
Degree does not have aluminium ion between 160-200g/L in tank liquor, stronger to oxidation film solvability.Usual anodizing time is
40-60 minutes, the molten aluminum amount of profile per ton was about 3.84Kg/T (400m2/T).With the accumulation of aluminium molten in tank liquor, Al3+To H+With
SO4 2-Footprint increase, seriously hinder H+To cathode, SO4 2-Ghandler motion is dynamic on the sunny side, the decline of tank liquor electric conductivity.Work as aluminium ion
When concentration reaches 20g/L or more, tank liquor resistance is too big, and according to constant voltage technique, current density is substantially reduced, and causes film layer thick
Degree is insufficient, transparency decline, or even white spot or the non-uniform phenomenons such as striped or the trace of other shapes occurs；According to
Constant current technique, and voltage can be caused to increase, power consumption increases, and blackening after film layer burn and closing is also possible that when serious
Phenomena such as.
Aluminium ion in anodizing solution directly affects the electric conductivity of tank liquor, determines oxidation energy consumption and film quality, most
Good controlled concentration should be between 3-8g/L range, and the oxidation film corrosion resistance that is obtained at this time, wearability are best.But in view of medicament at
This and environmental protection pressure, aluminium ion concentration general control is in the section 15-20g/L in actual production.
In view of aluminium ion concentration variation with coating mass and oxidation energy consumption just like this important relationship, aluminium processing enterprise one
As using two methods control aluminium ion.
First is that the method for slot outwells a part of tank liquor that is, when aluminium ion concentration is more than 20g/L, it is dense to reduce aluminium ion
Degree supplements sulfuric acid to 180g/L, continues to produce.Produce 100000 tons of anodic oxidation aluminum profiles per year, the molten aluminum amount of oxidation solution is 400 tons of left sides
The right side, 20000 tons or so of the oxidation waste liquid poured out every year, wherein containing 3600 tons of sulfuric acid, 400 tons of aluminium.Not only medicament is wasted, but also is born
The environmental protection pressure of the so a large amount of spent acid of processing and waste residue, also has lost more than 400 tons of recyclable bauxite resources.
Second is that using retrieval of sulfuric acid machine, as shown in Figure 2.Retrieval of sulfuric acid machine is aluminum ions stabilising arrangement, will using acid pump
The sulfuric acid of oxidation trough and the mixed liquor of aluminum sulfate are pumped into knockout drum since knockout drum is provided with the special material that cation exchanges
Material, quickly and efficiently separates sulfuric acid with aluminium ion, and aluminium ion is discharged except solution, sulfuric acid is sent back to and continues to make in oxidation trough
With, make except the aluminium ion constantly generated in production discharge solution, stablize the aluminium ion concentration in tank liquor in certain processing range,
And the sundries such as organic matter in tank liquor can be purified, longtime running no replacement is required tank liquor.Theoretically, which can make aluminium material oxidation
Film thickness and stay in grade, and energy conservation also provide good oxidation film basis to stablize profile coloring process.
But in actual operation, problem is many.In Fig. 2, certain model retrieval of sulfuric acid machine need to consume water about 1.5M3/H, consumption
Electricity about 3KW/H, i.e. monthly 1080 tons of water consumption, 2160 degree of power consumption.1080 tons of water that water outlet in Fig. 2 can be discharged in careful user
It measures, wherein sulfur acid 15-30g/L, aluminium ion 5-10g/L. have monthly discharged nearly 30 tons of sulfuric acid for discovery！Monthly so
The effect of water consumption power consumption, acquisition has few improvement than slot.
The using effect of the mirror such as above-mentioned bad luck of retrieval of sulfuric acid machine, most of aluminium processing enterprise gradually deactivates the device, extensive
The conventional method of a part oxidation tank liquor is answered.
Modern aluminum processing enterprise has anodic oxidation waste liquid in need of immediate treatment, and existing processing method is too simple.First is that straight
Run in and put wastewater treatment center into, not only increase processing cost, but also waste bauxite resource, also generates a large amount of industrial residue；Two
It is that professional treatment producer is asked to pull away.These treatment plants, if the oxidation acid pickle of single-item handling magnanimity, need to consume the lye of magnanimity,
Society can pay expensive processing cost thus.
As previously mentioned, the aluminium ion in anodizing solution, optium concentration should be controlled within the scope of 3-8g/L, be obtained at this time
Oxidation film corrosion resistance, wearability it is best, oxidation low energy consumption.Currently, the aluminium ion concentration in anodizing tank, each enterprise is basic
Control is between 15-20g/L, far beyond optium concentration section.Aluminium ion concentration is high, and resistance is big, and energy consumption is high, aoxidizes film quality
It is poor to measure, these are industry common recognitions.But it is limited by the environmental protection pressure of processing oxidation spent acid, enterprise is forced selection and improves aluminium ion control
The upper limit, using sacrificial oxidation film quality, increase energy consumption as cost, to reduce the discharge of oxidation spent acid.
In oxidation solution, there is Al3+、H+And SO4 2-, when not having added electric field, motion mode of these three ions in oxidation solution is two
Kind: vibration and drift.With Al3+For, motion mode are as follows:
(1), it is shaken in the spherical section centered on a certain equalization point, the maximum cross-section by the centre of sphere is its zone of influence
Domain, referred to as concussion section；
(2), next equalization point is floated to from an equalization point, then proceedes to shake, drift motion is named in this migration；Drift
Shifting be it is unordered, vibration is eternal；
After added electric field, each ion is in addition to drift and vibration, and there are also the directed movement along power line direction, concentration is gradually formed
Gradient distribution:
(3)、SO4 2-To anode movement after added electric field, forming anode, nearby concentration is high, and cathode nearby divide by the low gradient of concentration
Cloth；In anode, following electrochemical reaction is formed:
SO4 2-- 2e=2O+SO2↑ (losing electronics, discharge oxygen atom) (1)
2Al+3O=Al2O3(aluminium oxide alloy, oxygenerating film) (2)
Al2O3+3H+=2Al3++3OH-(oxidation film dissolution) (3)
(4)、Al3+、H+To cathode motion after added electric field, forming cathode, nearby concentration is high, the low gradient of concentration near anode
Distribution；In cathode, following electrochemical reaction is formed:
2H++ 2e=H2↑ (obtaining electronics, discharge hydrogen) (4)
Due to ionic radius difference, H+Prior to Al3+Cathode surface is reached, and due to current potential difference, H+It is preferential to obtain electronics,
Al3+It can only rest in oxidation solution and constantly accumulate.By (1) (4) formula it is found that the conductive capability at the two poles of the earth is the SO by anode4 2-
With the H at cathode+Concentration determine.With continuing for electrolysis, the ion near the two poles of the earth is constantly consumed, and needs the SO of distal end4 2-
And H+It is continuously replenished, makes to aoxidize lasting progress.At this moment, SO4 2-And H+The complexity mobile to the two poles of the earth, determines tank liquor conductive capability
The key problem of size, is directly determined by aluminium ion concentration.Assuming that a certain area for being parallel to the two poles of the earth is A's in oxidation solution
Section, the number at the aluminium ion vibration center passed through are N, each aluminum ions concussion section is S, then aluminium ion on the section
Total footprint be NS, SO4 2-And H+When by the section, being influenced lesser effective area by aluminium ion interception is A-NS.By
, it is found that aluminium ion concentration is higher, N is bigger for this, and effective area A-NS is smaller, SO4 2-And H+By difficulty it is bigger, tank liquor resistance
It is bigger.But according to (3) formula, aluminium ion concentration is reduced, reacts mobile to the right, oxidation film dissolution is accelerated, therefore aluminium ion concentration is not
It can be too low.Production practices prove that oxidation trough aluminium ion optium concentration is 3-8g/L, this section film layer is best, and tank liquor resistance is smaller,
Low energy consumption, and low energy consumption and high film quality, it is necessary to assure aluminium ion concentration is lower than 8g/L.For that purpose it is necessary to the aluminium of oxidation trough
Ion carries out specially treated, not only reduces aluminium ion, but also recycling sulfur acid oxidation solution and byproduct containing aluminium, and it is super thoroughly to solve aluminium ion
The drawbacks of outwelling a part of oxidation solution when crossing 20g/L.
In order to aoxidize energy conservation, other than reducing oxidation solution aluminium ion concentration, it is also necessary to oxidation trough configuration and oxidation solution sheet
Body carries out inhibition transformation, further increases energy-saving effect.
Existing oxidation trough is equipped with fixed negative pole plate and ice maker cooling system.
The distance between two cathode plates are depending on groove width, and general 1.6 meters or so, aluminium is as anode when oxidation, with cathode
The distance between plate is fixed as 0.8 meter.The energy of oxidation trough is inputted, a part does work to aluminium, aoxidizes aluminium, is converted to preparation
The chemical energy of oxidation film；A part is oxidized liquid absorption, causes tank liquor to heat up, aluminium alloy is most because tank liquor resistance generates thermal energy
Good oxidizing temperature is 18-22 DEG C, in order to guarantee continuous production, it is necessary to freeze, additionally increase energy consumption.The energy consumption heating of tank liquor resistance,
Need to consume energy refrigeration cool-down, dual energy consumption.Tank liquor resistance is reduced, i.e. shortening pole plate spacing and raising oxidation solution conductivity, had huge
The big energy saving space.
Coolant liquid generally enters from the bottom of oxidation trough, and upper surface two sides are overflowed, and takes heat out of to ice maker, completes cooling and follow
Ring.By (2) formula, aluminium alloy is oxidized to exothermic reaction, when oxidation solution temperature is 20 DEG C, aluminium alloy and oxidation solution interface
Temperature is higher than 20 DEG C, related with oxidate current beyond being worth.Current density is higher, and the temperature of aluminium material surface is higher, works as surface
When temperature is more than 30 DEG C (although just 20 DEG C of tank liquor temperature), oxidation film is burned.The temperature of interface aluminium material surface, limits oxygen
Galvanic current density cannot be too high, and when actual production, oxidation current generally takes 1.1-1.5A/dm2, oxidization time generally takes 40-60
Minute.By (3) formula, aluminium alloy anode oxide, while generate oxidation film, partial oxide film is dissolved.Interface temperature is higher,
Oxidization time is longer, sulfuric acid concentration is higher, and dissolved oxidation film is more.It is counted by large-scale production, 18-22 DEG C, anodic oxygen
Change 40-60 minutes, current density is 1.2 amperes/square decimeter, and the molten aluminum amount of profile per ton is about 3.84Kg/T (400m2/T).I.e.
400m2Aluminium surface, lose 3.84Kg aluminium, be converted into fine aluminium with a thickness of 3.56 microns.Oxidation film has double-layer structure, close to matrix
Metal be one layer of densification and it is thin, with a thickness of 0.01-0.05 μm of pure AL2O3Film, this layer are barrier layer；Outer layer is porous oxygen
Change film layer, by the AL with the crystallization water2O3Composition, that dissolved is the AL with the crystallization water2O3Oxidation film, rather than fine aluminium, thus it is molten
The oxide thickness numerical value of solution also will increase, at least at 3.56 microns or more.The type of cooling for improving oxidation trough, is transformed oxidation solution
Solvability, by reduce oxidation film meltage come it is energy saving, shorten oxidization time, raising effect, be to have very much strategic prospect
Research topic.
Chinese patent 201320875536.9 is proposed with the method that in mould liquid and anodizing solution recycles aluminium hydroxide is stewed, really
The aluminium hydroxide for meeting national standard GB4294-2010 requirement can be recycled in fact.But the method sacrifices the oxidation of this recoverable
Sulfuric acid in liquid, it is tangible unfortunate.It, can be chemically from oxidation solution by the method that Chinese patent 201410126857.8 provides
Individually crystallization aluminium ion, produces ammonium alum, and sulfuric acid all recycles.But the invention is set as only removing titanium exchanger except defrosting system
Frost, and when actual motion, corresponding pipeline, valve and pump are also required to defrost, therefore must do local directed complete set, will be arranged except defrosting system
To defrost to entire cooling system, rather than defrost only for titanium exchanger.It is provided by Chinese patent 201410126857.8
Method, can be recycled whole oxidation solutions, prevent down slot from this.Just because of not fall tank liquor, can trust and oxidation solution is audaciously transformed, increase
Add its corrosion inhibiting ability, reduces the meltage of oxidation film, further expand the energy saving space.
Summary of the invention
It is an object of the invention to propose oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saving technique, by mentioning
The aluminium in oxidation solution is taken, sulfuric acid is recycled, oxidation solution resistance is reduced, corrosion inhibiter is added in oxidation solution, reduces the dissolution of oxidation film
Amount aoxidizes energy conservation to realize.
It is another object of the present invention to propose oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saver,
20% or more energy conservation.
To achieve this purpose, the present invention adopts the following technical scheme:
Oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saving technique, including oxidation solution circulating cooling step, aluminium
Ionic crystal Product recycling step, sulfuric acid oxidation liquid recycling step, gas agitating step and defrosting step；
The oxidation solution circulating cooling step includes: using exchanger by the oxidation in the anodizing tank for handling aluminium alloy
Liquid cooling；
The aluminium ion crystalline product recycling step includes: that oxidation solution is imported reactor tank, and sulfuric acid is added into reactor tank
Ammonium aluminum sulfate crystal is precipitated after ammonium, then the material in reactor tank is imported in centrifuge to the solid being centrifuged after being separated by solid-liquid separation
And liquid；
The sulfuric acid oxidation liquid recycling step includes: the oxidation solution collected after crystallization treatment, is carried out at regeneration to oxidation solution
Anodizing tank recycling is delivered to after reason；
The gas agitating step includes: that ammonium sulfate is added into the reactor tank for fill oxidation solution, and stirring keeps its reaction abundant；
The defrosting step includes: dissolution and cleans the crystalline material in exchanger, and cleaning solution is imported in oxidation trough.
Further description, the regeneration treatment in the sulfuric acid oxidation liquid recycling step be added into oxidation solution it is organic
Corrosion inhibiter.
Further description, the organic inhibitor are organic acid or low mass molecule alcohol.
Further description, the addition concentration of the organic inhibitor are 30-50g/L.
Further description, the process being separated by solid-liquid separation in the aluminium ion crystalline product recycling step is under the conditions of spray
It carries out.
Oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saver, the inhibition energy saver includes oxidation solution
Circulating cooling system, aluminium ion crystalline product recovery system, sulfuric acid oxidation liquid recovery system, gas agitating system and remove defrosting system；
The oxidation solution circulating cooling system includes oxidation trough, refrigeration machine, titanium exchanger, No.1 pump and pipeline, the system
Cold cooperates the titanium exchanger to play refrigeration, and the tank liquor in the oxidation trough is imported the titanium and exchanged by the No.1 pump
Device is directed back again through pipeline to the oxidation trough by the oxidation solution that the titanium exchanger freezes；
The aluminium ion crystalline product recovery system includes reactor tank, centrifuge and pipeline, the feed inlet of the reactor tank
It is connected to by pipeline with No.1 pump, the discharge port of the reactor tank is connected to by pipeline with the centrifuge, the centrifugation
Machine is provided with water inlet pipe and water outlet, and the centrifuge is for separating and recovering crystalline solid；
The sulfuric acid oxidation liquid recovery system includes oxidation solution collecting pit, No. two pumps and pipeline, the oxidation solution collecting pit
Feed inlet be connected by pipeline with the centrifuge, the discharge port of the oxidation solution collecting pit passes through pipeline and described No. two
Pump connection, it is described No. two pump for by the oxidation solution of the oxidation solution collecting pit back to the oxidation trough；
The gas agitating system connectivity is in the reactor tank；
The defrosting system that removes includes the water inlet pipe that the drain into the titanium exchanger is pumped through the No.1, is exchanged from the titanium
The liquid of device outflow is transported in the oxidation trough.
Further description, the titanium exchanger are through type titanium exchanger, and the refrigeration machine is straight-through ice maker.
Further description, the centrifuge are the centrifuge with spray equipment, and the inlet of the spray equipment connects
It is connected to the water inlet pipe.
Further description, the water outlet of the centrifuge are provided with pH detector.
Beneficial effects of the present invention: by extracting the aluminium in oxidation solution, sulfuric acid is recycled, oxidation solution resistance is reduced, is aoxidizing
Corrosion inhibiter is added in liquid, reduces the meltage of oxidation film to realize oxidation energy conservation, 20% or more energy conservation.
Detailed description of the invention
Fig. 1 is the system structure diagram of one embodiment of the present of invention；
Fig. 2 is the structural schematic diagram for the retrieval of sulfuric acid machine that prior art oxidation trough is equipped with.
Wherein: oxidation trough 1, refrigeration machine 2, titanium exchanger 3, No.1 pump 4, reactor tank 5, centrifuge 6, oxidation solution collecting pit 7,
No. two pumps 8,07, No. eight valve of valve of valve 06, seven of valve 05, six of valve 04, five of valve 03, four of valve 02, three of No.1 valve 01, two
08,09, No. ten valve 010 of No. nine valves；
Oxidation trough 100, retrieval of sulfuric acid machine 101, infiltration ink 102, pump 103.
Specific embodiment
To further illustrate the technical scheme of the present invention below with reference to the accompanying drawings and specific embodiments.
The aluminum ions recycling of the application is by following theoretical foundation, quantitative analysis, waste liquid crystallization processing and aluminium ion and sulphur
Acid recovery system configuration is realized.
One, in anodizing solution aluminium ion and retrieval of sulfuric acid theoretical foundation
When oxidized aluminum alloy, (3) formula is pressed, partial oxide film is dissolved, about 4Kg/T (400m2) aluminium dissolve in sulfuric acid oxygen
Change liquid.Ammonium sulfate is added in this oxidation solution, then following reaction occurs:
Al2(SO4)3+(NH4)2SO4+12H2O=2NH4Al(SO4)2·12H2O↓ (3)
Under the conditions of 160-200g/L sulfuric acid, ammonium are excessive, alum NH4Al(SO4)2·12H2O crystallization is precipitated, residual
It stays aluminum ions how much related with crystallization temperature and time.
Two, quantitative analytical experiment result
1 liter of anodizing solution is taken, free sulfuric acid 183.9g/L, Al3+20.20g/L, conductivity 152.5s/m, 25 DEG C of temperature,
Addition ammonium sulfate is tested.Crystallization after twenty minutes, measures sulfuric acid concentration, aluminium ion concentration and the conductivity of tank liquor, knot in time
Fruit is as shown in table 1:
1 bath parameters of table with various concentration ammonium sulfate changing rule
By (5) formula, every crystallization 1g/L Al3+, need to add 2.45g/L ammonium sulfate, the initial Al of oxidation solution3+20.20g/L,
Ammonium sulfate 49.49g/L need to be consumed by being fully crystallized precipitation.Table 1 and its experiments supporting show:
1, ammonium sulfate is added in oxidation solution, under room temperature, crystallizable precipitation alum in the short time；
2, with the increase of ammonium sulfate additive amount, aluminium ion is gradually reduced, but the range of decrease narrows；
3, as crystallization time increases, aluminium ion is further decreased；
4, as crystallization temperature reduces, aluminium ion concentration is reduced；
Even if 5, ammonium ion is excessive, low temperature and long-time crystallize, aluminium ion can not be fully crystallized precipitation；
6, with the increase of ammonium sulfate additive amount, sulfuric acid concentration increases；
7, with the increase of ammonium sulfate additive amount, conductivity increases.
Three, aluminium alloy anode oxide slot aluminium ion and retrieval of sulfuric acid Process configuration
It is practical in conjunction with oxidation line quantity-produced according to reaction equation (5) and the experimental result of table 1, retrieval of sulfuric acid, byproduct
The factors such as collection, packaging, and idle place etc., oxidation trough aluminium ion recovery process and configuration are designed by Fig. 1.
This recovery system produces 100000 tons of aluminum profiles per year by the aluminium oxide profile design for producing 100000 tons per year, generates oxidation waste liquid
20000 tons, molten aluminum amount is 400 tons or so.
In order to realize the target of 20000 tons of oxidation waste liquids of processing, 1 40M is configured in attached drawing3Oxidation waste liquid reactor tank, 1
40M3Oxidation solution collecting pit, a desk centrifuge and matched pipeline, pump and valve.
Individually oxidation liquid waste processing area should be arranged in the characteristics of being not easy long-distance pipeline in view of oxidation solution, this system
Domain facilitates treated oxidation solution directly returning oxidation trough with pipeline close to oxidation workshop.
With oxidation the waste liquid reactor tank, pump, valve and the pipeline that contacts, it is necessary to press acidproof design, it is contemplated that aoxidize waste liquid regardless of
Solution does not block pipeline and valve, selects acid-proof pump, and from oxidation trough stringing and valve, oxidation waste liquid is evacuated to reactor tank.
Gas agitating is only set in reactor tank, allow for chemical reaction it is fairly simple, be uniformly mixed.According to electricity
Machine stirring, not only power consumption, but also it is dangerous, it repairs more troublesome.
Whole aluminium alloy anode oxide slot aluminium ion and retrieval of sulfuric acid technique, including oxidation solution circulating cooling step, aluminium
Ionic crystal Product recycling step, sulfuric acid oxidation liquid recycling step, gas agitating step and defrosting step；
The oxidation solution circulating cooling step includes: using exchanger by the oxidation in the anodizing tank for handling aluminium alloy
Liquid cooling；
The aluminium ion crystalline product recycling step includes: that oxidation solution is imported reactor tank, and sulfuric acid is added into reactor tank
Ammonium aluminum sulfate crystal is precipitated after ammonium, then the material in reactor tank is imported in centrifuge to the solid being centrifuged after being separated by solid-liquid separation
And liquid；
The sulfuric acid oxidation liquid recycling step includes: the oxidation solution collected after crystallization treatment, is carried out at regeneration to oxidation solution
Anodizing tank recycling is delivered to after reason；
The gas agitating step includes: that ammonium sulfate is added into the reactor tank for fill oxidation solution, and stirring keeps its reaction abundant；
The defrosting step includes: dissolution and cleans the crystalline material in exchanger, and cleaning solution is imported in oxidation trough.
Solid after separation of solid and liquid is ammonium aluminum sulfate crystal, and liquid is the oxidant of sulfur acid.
Further description, the regeneration treatment in the sulfuric acid oxidation liquid recycling step be added into oxidation solution it is organic
Corrosion inhibiter.Using the corrosion inhibition of organic inhibitor, under identical oxidizing condition, by reducing the meltage of oxidation film, increase
2 microns of oxide thickness or more, ton material economizes on electricity 200 degree or more.On the basis of crystallizing aluminium ion, all recycling oxidation solutions,
Organic acid is added in oxidation solution, using its corrosion inhibiting ability, reduces the dissolution of oxidation film, realizes oxidation energy conservation.
Further description, the organic inhibitor are organic acid or low mass molecule alcohol.Organic acid can be tartaric acid, Portugal
Grape saccharic acid, lactic acid, oxalic acid or citric acid etc., low mass molecule alcohol can be sorbierite or ethylene glycol.
Further description, the addition concentration of the organic inhibitor are 30-50g/L.
Further description, the process being separated by solid-liquid separation in the aluminium ion crystalline product recycling step is under the conditions of spray
It carries out.
Further description, as shown in Figure 1, the inhibition section of aluminium alloy anode oxide slot aluminium ion and retrieval of sulfuric acid technique
Energy device, the inhibition energy saver includes oxidation solution circulating cooling system, aluminium ion crystalline product recovery system, sulfuric acid oxidation
Liquid recovery system, gas agitating system and remove defrosting system；
The oxidation solution circulating cooling system includes oxidation trough 1, refrigeration machine 2, titanium exchanger 3, No.1 pump 4 and pipeline, institute
Stating refrigeration machine 2 cooperates the titanium exchanger 3 to play refrigeration, and the tank liquor in the oxidation trough is imported institute by the No.1 pump 4
Titanium exchanger 3 is stated, is directed back again through pipeline to the oxidation trough 1 by the oxidation solution that the titanium exchanger 3 freezes；
The aluminium ion crystalline product recovery system includes reactor tank 5, centrifuge 6 and pipeline, the charging of the reactor tank 5
Mouth is connected to by pipeline with No.1 pump 4, and the discharge port of the reactor tank 5 is connected to by pipeline with the centrifuge 6, described
Centrifuge 6 is provided with water inlet pipe and water outlet, and the centrifuge is for separating and recovering crystalline solid；
The sulfuric acid oxidation liquid recovery system includes oxidation solution collecting pit 7, two pumps 8 and pipeline, and the oxidation solution is collected
The feed inlet in pond 7 is connected by pipeline with the centrifuge 6, and the discharge port of the oxidation solution collecting pit 7 passes through pipeline and institute
8 connection of No. two pumps is stated, No. two pumps 8 are used for the oxidation solution of the oxidation solution collecting pit 7 back to the oxidation trough 1；
The gas agitating system connectivity is in the reactor tank；
The defrosting system that removes includes the water inlet pipe through the drain into the titanium exchanger 3 of No.1 pump 4, is handed over from the titanium
The liquid that parallel operation 3 flows out is transported in the oxidation trough 1.
No.1 pump 4 is connected to titanium exchanger 3, oxidation trough 1 and reactor tank 5 by triple valve, in order to ensure hereafter retouching
State clear errorless, the valve for now enabling No.1 pump 4 communicate with titanium exchanger 3 is No. two valves 02, the valve of No.1 pump 4 and oxidation trough 1
For No.1 valve 01, the valve of No.1 pump 4 and reactor tank 5 is No. three valves 03, is provided with No. ten valves 010 on the water inlet pipe of centrifuge,
Valve between No. two pumps 8 and oxidation trough 1 is No. seven valves 07, and the valve between oxidation solution collecting pit 7 and No. two pumps 8 is No. six valves
06, the valve between titanium exchanger 3 and oxidation trough 1 is No. four valves 04, and the valve between reactor tank 5 and centrifuge 6 is No. five valves
05, the valve between gas agitating system and reactor tank 5 is No. eight valves 08.
It is specific:
(1), oxidation solution circulating cooling step: it is responsible for circulating cooling oxidation solution；Operating procedure are as follows: close No. three valves and No. nine
The valve of valve, the valve for opening 01, No. two valve 02 of No.1 valve and No. four valves 04 and starting No.1 pump 4 and refrigeration machine 2, make to aoxidize
Slot 1 cools down；
(2), aluminium ion crystallization auxiliary Product recycling step: it is responsible for collecting storage oxidation waste liquid, in the condition of addition ammonium sulfate
Under, alum is precipitated in crystallization, and the separation of solid and liquid of alum byproduct is carried out under the conditions of spray.Operating procedure are as follows: a,
The valve for opening No. three valves 03 closes the valve of No. two valves 02 and No. nine valves 09, by 30M3After oxidation solution is evacuated to reactor tank, open
No. two valves 02 close No. three valves 03；No. eight valves 08 for opening gas agitating system, start to stir；By 2.5 times of weights of aluminium ion concentration
Amount adds ammonium sulfate, stirring while adding；Ammonium sulfate adds, and closes No. eight valves 08 after continuing stirring 30 minutes, stands 2 hours；
B, No. five valves 05 are opened, crystalline solid enters centrifuge.Centrifuge 6 is opened, is separated by solid-liquid separation；Open No. ten valves 010, to from
Solid in scheming 6 sprays repeatedly, when the pH value of 6 water outlet recovered liquid of centrifuge is greater than 4.5, closes No. ten valves 010, stops
Spray and centrifuge 6 recycle alum byproduct；
(3), sulfuric acid oxidation liquid recycling step: being responsible for collecting the oxidation solution after crystallization treatment, and is delivered to oxidation trough circulation
It uses.Operating procedure are as follows: 06, No. seven valve 07 of No. six valves and No. two pumps 8 are opened, sends the oxidation solution of reclaiming back to oxidation trough 1,
Complete retrieval of sulfuric acid；
(4), gas agitating step: it is responsible for sulfuric acid oxidation liquid and ammonium sulfate mixed dissolution, sufficiently reacts.Operating procedure are as follows: beat
No. eight valves 08 of gas agitating are opened, start to stir；By 2.5 times of weight of aluminium ion concentration, ammonium sulfate is added, it is stirring while adding；Sulphur
Sour ammonium adds, and closes No. eight valves 08 after continuing stirring 30 minutes, stands 2 hours；
(5), defrosting step: it is responsible for cleaning dissolution No.1 pump 4, the valve 04 of valve 02, four of No.1 valve 01, two, titanium exchanger 3
And the alum crystallization of pipeline, restore heat exchanger effectiveness, and cleaning solution is delivered to oxidation trough 1, supplement oxidation tank liquor position.Behaviour
Make step are as follows: close refrigeration machine 6 and No.1 pump 4；01, No. three valve 03 of No.1 valve is closed, 09, No. two valve 02 and four of No. nine valves is opened
Number valve 04 is crystallized with the alum that tap water cleans cooling titanium tube surface in dissolution No.1 pump 4 and titanium exchanger 3, improves heat
Exchange efficiency, and cleaning solution is delivered to oxidation trough 1, (alum contains 12 crystallizations water, oxidation solution to supplement 1 liquid level of oxidation trough
Position dehydration is serious, cleaning cooling system just moisturizing).
Aluminium ion crystallization is precipitated, oxidation solution is recycled, and has avoided the huge of sulfuric acid and bauxite resource caused by outwelling oxidation solution
Big waste, reduces the environmentally friendly cost for handling these waste liquids and waste residue.By table 1, aluminum ions reduction, it is meant that tank liquor resistance
It reduces.In table 1, Al3+When 20.20g/L, conductivity 152.5s/m；Al3+When 9.00g/L, conductivity 164.25s/m.Conductivity
Increase by 7.7%, i.e. oxidation solution resistance reduces by 7.7%.Aluminium processing enterprise aoxidizes one ton of aluminium, consumes about 1000 degree of electricity, reduces
7.7% resistance, it is meant that less with 77 degree of electricity；When passing through in view of electric current, tank liquor resistance makes tank liquor heat up, and also ice maker is needed to cool down
Energy consumption, crystallization aluminium ion reduce tank liquor resistance, reduce cooling energy consumption, and energy-saving index can further improve.
Corrosion inhibiter can be added in oxidation solution, reduces the molten of oxidation film not falling slot under the premise of recycling oxidation solution completely
Xie Liang, further energy conservation.By (3) formula, aluminium alloy anode oxide, while generate oxidation film, partial oxide film is dissolved.Interface
Place's temperature is higher, oxidization time is longer, sulfuric acid concentration is higher, and dissolved oxidation film is more.It is counted by large-scale production, 18-
22 DEG C, anodic oxidation 40-60 minutes, current density was 1.2 amperes/square decimeter, and the molten aluminum amount of profile per ton is about 3.84Kg/T
(400m2/ T), generate 12 μm or so of oxidation film.That is 400m2Aluminium surface, lose 3.84Kg aluminium, be converted into fine aluminium with a thickness of
3.56 micron.Oxidation film has double-layer structure, close to parent metal be one layer of densification and it is thin, it is pure with a thickness of 0.01-0.05 μm
AL2O3Film, this layer are barrier layer；Outer layer is porous oxidation film layer, by the AL with the crystallization water2O3Composition, dissolved is band knot
The AL of brilliant water2O3Oxidation film, rather than fine aluminium, therefore oxide thickness numerical value also will increase, at least at 3.56 microns or more.Dissolution
Oxidation film and the ratio between the oxidation film of generation be (3.56 μm/12 μm) 0.297, can also so understand, that is, collectively generate 15.56
μm oxidation film, wherein 3.56 μm be dissolved, 12 μm remain, dissolving ratio 22.88%.In recycling oxidation solution completely
Under the premise of, corrosion inhibiter, such as tartaric acid, gluconic acid, lactic acid, oxalic acid, citric acid and low molecule can be added in oxidation trough
Alcohol, such as sorbierite, ethylene glycol, using the corrosion inhibition of these organic principles, by reduce the meltage of oxidation film come it is energy saving,
Shorten oxidization time and improves effect.Take free sulfuric acid 206.19g/L, Al3+When 9.00g/L, conductivity 164.25s/m, temperature
20 DEG C, anodizing time 40 minutes, current density was 1.2 amperes/square decimeter, and adding different organic matters, (concentration is
Oxidation control experiment 30g/L) is carried out, detects average film thickness, the results are shown in Table 2:
Table 2 adds influence of the different organic matters to anodic oxidation film thickness
Using oxalic acid as corrosion inhibiter, free sulfuric acid 206.19g/L is taken, when Al3+9.00g/L, conductivity 164.25s/m, temperature
20 DEG C, anodizing time 40 minutes, current density was 1.2 amperes/square decimeter, studied different concentration of oxalic acid to average oxidation
The influence of film thickness, the results are shown in Table 3:
Influence of the different concentration of oxalic acid of table 3 to oxide thickness
Table 3 shows addition organic inhibitor, can increase oxide thickness, wherein tartaric acid, lactic acid, oxalic acid and citric acid
It performs better than.Table 3 shows to increase with concentration of oxalic acid, and oxide thickness increases, when concentration of oxalic acid reaches 40g/L or more, film thickness
Increase it is limited, therefore appropriate organic acid concentration be 30-50g/L.
Add solution rate of the organic matter for reducing oxidation film, identical oxidizing condition, can increase by 2 μm of oxidation film with
On, 200 degree of economize on electricity or more reduces the meltage of oxidation film, is energy-efficient effective way.The present invention passes through crystallization aluminium ion, drop
Low tank liquor resistance, ton material economize on electricity 70 degree or more, and by addition organic acid, reduce the meltage of oxidation film, 200 degree of economize on electricity with
On, it is contemplated that the energy consumption for cooling of reduction due to reducing tank liquor resistance realizes oxidation economize on electricity according to both effective energy conservation measures
20% or more.
Organic acid is added in oxidation solution, protects oxidation film, is reduced meltage, is a traditional energy conservation measure, but so far
Fail popularity, basic reason is that the aluminium ion problem in oxidation solution could not be solved thoroughly.Using retrieval of sulfuric acid machine shown in Fig. 2
Method, organic matter may block permeable membrane in tank liquor, and retrieval of sulfuric acid machine is made to fail；Using partial oxidation liquid method is outwelled, can incite somebody to action
Deliberately be added to oxidation solution, expensive organic acid outwell together, cost is too big, and opposite energy-saving benefit may lose more than gain.Only
Have the technological means that whole oxidation solutions are recycled by crystallization aluminium ion of the invention, could to add in oxidation solution organic acid,
Oxidation film dissolution is reduced, practicable power-saving technology is become.
Further description, the titanium exchanger are through type titanium exchanger, and the refrigeration machine is straight-through ice maker.This work
Refrigeration machine 6 selects straight-through ice maker in skill configuration, or is transformed to existing refrigeration machine, removes plate heat exchanger, uses refrigerating fluid instead
Pass through the direct-cooled titanium exchanger of titanium tube.Aluminium ion in actual production, ammonium ion cannot be precipitated completely, can be with one piece of retrieval of sulfuric acid liquid
Into oxidation tank liquor.According to plate heat exchanger, alum can be precipitated in the stenosis of plate heat exchanger, block exchanger,
It is cooling to influence oxidation solution, causes to stop production.When selecting titanium exchanger, since refrigerant recycles in titanium tube, directly contacted outside titanium tube
Oxidation solution both improves heat exchanger effectiveness, reduces energy consumption, and has thoroughly prevented the hidden danger that blocking exchanger is precipitated in alum.
Further description, the centrifuge are the centrifuge with spray equipment, and the inlet of the spray equipment connects
It is connected to the water inlet pipe.
The water outlet of further description, the centrifuge 6 is provided with pH detector.It is provided with pH detector, it is right
The pH value of water outlet recovered liquid carries out examinations, when it is greater than 4.5, closes No. ten valves 010, stop spray equipment and from
Alum byproduct is recycled in scheming.
Embodiment
The recycling of aluminium ion and sulfuric acid and oxidation solution inhibition reducing energy consumption in aluminium alloy anode oxide waste liquid are added according to aluminium
Work enterprise generates largely useless oxidation solution every year, not only increases processing cost, but also the status of waste bauxite resource, online design is direct for the first time
Crystallization treatment is given up oxidation solution, recycles sulfuric acid, aluminium ion is completely converted into the alum of technical grade.Aluminum ions reduction, drop
Low oxidation solution resistance is, it can be achieved that 7% or more oxidation energy conservation.On the basis of oxidation solution obtains all recycling, the present invention is in oxygen
Change in liquid and add organic inhibitor, reduces the dissolution of oxidation film, 20% or more energy conservation.The present invention aoxidizes liquid waste processing and byproduct
Recycling, oxidation energy conservation object are achieved, and system configuration and science operation are successful keys.
Embodiment 1 (aluminium alloy anode oxide continuous production)
It closes 03, No. nine valve 09 of No. three valves, open the valve 02, four of No.1 valve 01, two valve 04, No.1 pump 4 and refrigeration machine,
Oxidation trough cooling, oxidation line start to produce；
Embodiment 2 (online recycling alum)
1, No. three valves 03 are opened, 02, No. nine valve 09 of No. two valves are closed, by 30M3After oxidation solution is evacuated to reactor tank, two are opened
Number valve 02, closes No. three valves 03；No. eight valves 08 of gas agitating are opened, start to stir；By 2.5 times of weight of aluminium ion concentration, addition
Ammonium sulfate, it is stirring while adding；Ammonium sulfate adds, and closes No. eight valves 08 after continuing stirring 30 minutes, stands 2 hours；
2, No. five valves 05 are opened, crystalline solid enters centrifuge.Centrifuge is opened, is separated by solid-liquid separation；Open No. ten
Valve 010 sprays the solid in centrifuge repeatedly, when the pH value of centrifuge water outlet recovered liquid is greater than 4.5, closes No. ten valves
010, stop spray and centrifuge, recycles alum byproduct；
Embodiment 3 (online recycling oxidation solution)
06, No. seven valve 07 of No. six valves and No. two pumps 8 are opened, the oxidation solution of reclaiming is sent back to oxidation trough, completes sulfuric acid
Recycling；
Embodiment 4 (cooling system defrosting)
Close refrigeration machine and variable frequency pump；01, No. three valve 03 of No.1 valve is closed, the valve of valve 02, four of No. nine valves 09, two is opened
04, it is crystallized with the alum that tap water cleans cooling titanium tube surface in dissolution variable frequency pump and titanium exchanger, improves heat exchange effect
Rate, and cleaning solution is delivered to oxidation trough, supplement oxidation tank liquor position；
Embodiment 5 (oxidation solution transformation)
Oxalic acid 10g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 6 (oxidation solution transformation)
Oxalic acid 20g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 7 (oxidation solution transformation)
Oxalic acid 30g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 8 (oxidation solution transformation)
Oxalic acid 40g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 9 (oxidation solution transformation)
Oxalic acid 50g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 10 (oxidation solution transformation)
Tartaric acid 40g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 11 (oxidation solution transformation)
Citric acid 40g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 12 (oxidation solution transformation)
Lactic acid 40g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 13 (oxidation solution transformation)
Gluconic acid 40g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square
Decimetre, anodizing time 35 minutes；
Embodiment 14 (oxidation solution transformation)
Sorbierite 40g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes；
Embodiment 15 (oxidation solution transformation)
Ethylene glycol 40g/L, free sulfuric acid 180g/L, Al3+10g/L, 20 DEG C of temperature, current density is 1.2 amperes/square point
Rice, anodizing time 35 minutes.
The technical principle of the invention is described above in combination with a specific embodiment.These descriptions are intended merely to explain of the invention
Principle, and shall not be construed in any way as a limitation of the scope of protection of the invention.Based on the explanation herein, the technology of this field
Personnel can associate with other specific embodiments of the invention without creative labor, these modes are fallen within
Within protection scope of the present invention.
Claims (5)
1. oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saving technique, it is characterised in that: recycled including oxidation solution cold
But step, aluminium ion crystalline product recycling step, sulfuric acid oxidation liquid recycling step, gas agitating step and defrosting step；
Specifically,
(1) oxidation solution circulating cooling step: it is responsible for circulating cooling oxidation solution；Operating procedure are as follows: close No. three valves and No. nine valves
Valve, the valve for opening No.1 valve, No. two valves and No. four valves and starting No.1 pump and refrigeration machine, make oxidation trough cool down；
(2) aluminium ion crystallization auxiliary Product recycling step: it is responsible for collecting storage oxidation waste liquid, under conditions of adding ammonium sulfate, knot
Partial crystallization goes out alum, and the separation of solid and liquid of alum byproduct, operating procedure are carried out under the conditions of spray are as follows: a, opens three
The valve of number valve, closes the valve of No. two valves and No. nine valves, after oxidation solution is evacuated to reactor tank, opens No. two valves, closes No. three
Valve；No. eight valves for opening gas agitating system, start to stir；By 2.5 times of weight of aluminium ion concentration, ammonium sulfate, side edged are added
Stirring；Ammonium sulfate adds, and closes No. eight valves after continuing stirring 30 minutes, stands 2 hours；B, No. five valves, crystalline solid are opened
Into centrifuge；Centrifuge is opened, is separated by solid-liquid separation；No. ten valves are opened, the solid in centrifuge is sprayed repeatedly, works as centrifugation
When the pH value of machine water outlet recovered liquid is greater than 4.5, No. ten valves are closed, stop spray and centrifuge, recycle alum byproduct；
(3) sulfuric acid oxidation liquid recycling step: being responsible for collecting the oxidation solution after crystallization treatment, and is delivered to oxidation trough recycling,
Operating procedure are as follows: open No. six valves, No. seven valves and No. two pumps, send the oxidation solution of reclaiming back to oxidation trough, complete sulfuric acid and return
It receives；
(4) gas agitating step: it is responsible for sulfuric acid oxidation liquid and ammonium sulfate mixed dissolution, sufficiently reacts, operating procedure are as follows: open gas mixing
No. eight valves are mixed, start to stir；By 2.5 times of weight of aluminium ion concentration, ammonium sulfate is added, it is stirring while adding；Ammonium sulfate adds,
No. eight valves are closed after continuing stirring 30 minutes, stand 2 hours；
(5) defrosting step: it is responsible for cleaning dissolution No.1 pump, No.1 valve, No. two valves, No. four valves, the sulfuric acid of titanium exchanger and pipeline
Aluminium crystalline ammonium restores heat exchanger effectiveness, and cleaning solution is delivered to oxidation trough, supplement oxidation tank liquor position, operating procedure are as follows: close
Refrigeration machine and No.1 pump；No.1 valve, No. three valves are closed, No. nine valves, No. two valves and No. four valves are opened, cleans dissolution one with tap water
The alum crystallization on cooling titanium tube surface in number pump and titanium exchanger, and cleaning solution is delivered to oxidation trough, supplement oxidation trough
Liquid level；
Wherein, the regeneration treatment in the sulfuric acid oxidation liquid recycling step is that organic inhibitor is added into oxidation solution；It is described to have
Machine corrosion inhibiter is tartaric acid, lactic acid, oxalic acid and citric acid；The addition concentration of the organic inhibitor is 30-50g/L.
2. oxygen used in oxidation trough aluminium ion according to claim 1 and retrieval of sulfuric acid and oxidation solution inhibition energy saving technique
Change slot aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saver, it is characterised in that: the inhibition energy saver includes oxidation
Liquid circulating cooling system, aluminium ion crystalline product recovery system, sulfuric acid oxidation liquid recovery system, gas agitating system and defrosting system
System；
The oxidation solution circulating cooling system includes oxidation trough, refrigeration machine, titanium exchanger, No.1 pump and pipeline, the refrigeration machine
The titanium exchanger is cooperated to play refrigeration, the tank liquor in the oxidation trough is imported the titanium exchanger by the No.1 pump,
It is directed back again through pipeline to the oxidation trough by the oxidation solution that the titanium exchanger freezes；
The aluminium ion crystalline product recovery system includes reactor tank, centrifuge and pipeline, and the feed inlet of the reactor tank passes through
Pipeline is connected to No.1 pump, and the discharge port of the reactor tank is connected to by pipeline with the centrifuge, and the centrifuge is set
It is equipped with water inlet pipe and water outlet, the centrifuge is for separating and recovering crystalline solid；
The sulfuric acid oxidation liquid recovery system include oxidation solution collecting pit, No. two pump and pipeline, the oxidation solution collecting pit into
Material mouth is connected by pipeline with the centrifuge, and the discharge port of the oxidation solution collecting pit is connected by pipeline and No. two pumps
It is logical, No. two pumps for by the oxidation solution of the oxidation solution collecting pit back to the oxidation trough；
The gas agitating system connectivity is in the reactor tank；
The defrosting system that removes includes the water inlet pipe that the drain into the titanium exchanger is pumped through the No.1, from the titanium exchanger stream
Liquid out is transported in the oxidation trough.
3. oxidation trough aluminium ion according to claim 2 exists with retrieval of sulfuric acid and oxidation solution inhibition energy saver, feature
In: the titanium exchanger is through type titanium exchanger, and the refrigeration machine is straight-through ice maker.
4. oxidation trough aluminium ion according to claim 2 exists with retrieval of sulfuric acid and oxidation solution inhibition energy saver, feature
In: the centrifuge is the centrifuge with spray equipment, and the inlet of the spray equipment is connected to the water inlet pipe.
5. oxidation trough aluminium ion according to claim 2 exists with retrieval of sulfuric acid and oxidation solution inhibition energy saver, feature
In: the water outlet of the centrifuge is provided with pH detector.
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| CN103911651A (en) * | 2014-03-28 | 2014-07-09 | 佛山市三水雄鹰铝表面技术创新中心有限公司 | Process for recovering aluminum ions and sulfuric acid from aluminum alloy anodic oxidation tank |
| CN105803506A (en) * | 2016-03-28 | 2016-07-27 | 佛山市三水雄鹰铝表面技术创新中心有限公司 | Fluoride-free and ammonium-free four-in-one recovery system for pretreatment chemicals of sand surface of aluminum alloy |
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| WO2011145033A1 (en) * | 2010-05-21 | 2011-11-24 | Massimiliano Gazzani | A method and a system for anodising a profiled section made of aluminium or alloys thereof |
| CN103911651A (en) * | 2014-03-28 | 2014-07-09 | 佛山市三水雄鹰铝表面技术创新中心有限公司 | Process for recovering aluminum ions and sulfuric acid from aluminum alloy anodic oxidation tank |
| CN105803506A (en) * | 2016-03-28 | 2016-07-27 | 佛山市三水雄鹰铝表面技术创新中心有限公司 | Fluoride-free and ammonium-free four-in-one recovery system for pretreatment chemicals of sand surface of aluminum alloy |
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