CN107858731A - A kind of oxidized aluminum alloy liquid recovery and cooling device crystallization removing system and technique - Google Patents
A kind of oxidized aluminum alloy liquid recovery and cooling device crystallization removing system and technique Download PDFInfo
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- CN107858731A CN107858731A CN201711256760.9A CN201711256760A CN107858731A CN 107858731 A CN107858731 A CN 107858731A CN 201711256760 A CN201711256760 A CN 201711256760A CN 107858731 A CN107858731 A CN 107858731A
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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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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25D—PROCESSES FOR THE ELECTROLYTIC OR ELECTROPHORETIC PRODUCTION OF COATINGS; ELECTROFORMING; APPARATUS THEREFOR
- 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
The invention discloses a kind of recovery of oxidized aluminum alloy liquid and cooling device crystallization removing system, including oxidation solution collection system, oxidation liquid treating system, oxidation liquid separation system, washing medicament retention system and cooling device crystallization removing system.Reclaimed the invention also discloses a kind of oxidized aluminum alloy liquid and cooling device crystallizes and removes technique, including oxidation solution is collected, oxidation solution is handled, oxidation solution separates, oxidation solution reclaims, recrystallization recycling step, washing medicament retain, cooling device crystallizes removing.The system and the technique oxidation solution rate of recovery of the present invention is high；Realize low level dosing；Large-scale industrial production demand can be met；Saving water resource.
Description
Technical field
The present invention relates to the technical field of aluminum Product processing, more particularly to a kind of recovery of oxidized aluminum alloy liquid to set with cooling
Standby crystallization removing system and technique.
Background technology
Aluminium alloy anode oxide wire casing position is arranged as shown in Figure 1 in the prior art.In 10# groove anodizing solutions, have
The aluminium alloy of conductive surface is placed in anode, and under External Electrical Field, the process that surface forms oxide-film is referred to as anodic oxidation, is produced
Raw film is anode oxide film or is electrochemically transformed film.Electrochemical oxidation film is different from Natural Oxide Film, and oxide-film is thin for accumulation
Born of the same parents' structure, each cell are a hexagonal cylinder, and its top is a circular arc and has the pore truncation surface of hexagram.Oxidation
Film has double-layer structure, close to parent metal be one layer of densification and it is thin, thickness is 0.01-0.05 μm of pure AL2O3Film, hardness is high,
This layer is barrier layer；Outer layer is porous oxidation film layer, by the AL with the crystallization water2O3Composition, hardness are relatively low.Electrochemical oxidation is pressed
The main component of electrolyte can be divided into:Sulphuric acid anodizing, oxalic acid anodizing, chromic acid anodizing；By the function of oxide-film
It can be divided into:Wear-resisting film layer, corrosion-resistant film layer, it is glued film layer, insulating film layer, porcelain film layer and decoration oxidation.Aluminium alloy is through anode
After oxidation processes, the oxide-film characterized by porous is formed in aluminium material surface, it is necessary to by sealing pores, to ensure aluminium alloy
The physical and chemical performances such as corrosion resistance, weatherability and the wearability of anodic oxidation product, obtain durable performance.
Alumilite process liquid refers to the tank liquor used in aluminium alloy anode oxide.During fluting, anodizing solution H2SO4Concentration exists
Between 160-200g/L, there is no aluminium ion in tank liquor, it is stronger to oxide-film solvability.Usual anodizing time is 40-60
Minute, temperature is 18-22 DEG C, and the molten aluminum amount of section bar per ton is about 3.84Kg/T (400m2/T).With the accumulation of molten aluminium in tank liquor,
Al3+To H+And SO4 2-Footprint increase, seriously hinder H+To negative electrode, SO4 2-Ghandler motion moves on the sunny side, and tank liquor electric conductivity declines.
When aluminium ion concentration reaches more than 20g/L, tank liquor resistance is too big, and according to constant voltage technique, current density substantially reduces, and makes
Film forming layer thickness deficiency, transparency decline, or even the white spot of appearance or striped or the vestige of other shapes etc. are uneven existing
As；According to constant current technique, voltage can be caused to raise again, power consumption increase, be also possible that when serious film layer burn and
After closing phenomena such as blackening.
Aluminium ion in anodizing solution, the electric conductivity of tank liquor is directly affected, determine oxidation energy consumption and film quality, most
Good controlled concentration should be between 3-8g/L scopes, and the oxidation film corrosion resistance that is now obtained, wearability are best.But in view of medicament into
Sheet and environmental protection pressure, aluminium ion concentration general control is in 15-20g/L sections in actual production.
In view of aluminium ion concentration change and coating mass and oxidation energy consumption are just like this important relation, aluminium processing enterprise one
As using two methods control aluminium ion.
First, the method for groove, i.e., when aluminium ion concentration is more than 20g/L, outwell a part of tank liquor, it is dense to reduce aluminium ion
Degree, supplement sulfuric acid continue to produce to 180g/L.Produce 100000 tons of anodic oxidation aluminium section bars 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.Both medicament is wasted, is born again
The environmental protection pressure of the so a large amount of spent acid of processing and waste residue, also have lost more than 400 tons of recyclable aluminum metal.
Second, retrieval of sulfuric acid machine is used, as shown in Figure 3.Retrieval of sulfuric acid machine is aluminum ions stabilising arrangement, using sour pump
The mixed liquor of the sulfuric acid of oxidation trough and aluminum sulfate is pumped into knockout drum because knockout drum is built with the special material of cation exchange
Material, quickly and efficiently separates sulfuric acid with aluminium ion, and aluminium ion is discharged outside solution, sulfuric acid is sent back in oxidation trough and continues to make
With, make in production constantly caused by outside aluminium ion discharge solution, aluminium ion concentration in stable tank liquor in certain processing range,
And the debris such as organic matter in tank liquor can be purified, longtime running need not change tank liquor.Theoretically, the device can make aluminium material oxidation
Film thickness and stay in grade, and save, also provide good oxide-film basis to stablize section bar coloring process.
But in actual motion, problem is many.In Fig. 3, 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 careful user can discharge to delivery port in Fig. 2
Measure, it is found that wherein sulfur acid 15-30g/L, aluminium ion 5-10g/L. have monthly discharged nearly 30 tons of sulfuric acid.It is monthly such
Water consumption power consumption, the effect of acquisition have few improvement than groove.
The mirror such as above-mentioned bad using effect of retrieval of sulfuric acid machine, most of aluminium processing enterprise, progressively disables the device, extensive
The conventional method of part oxidation tank liquor is answered.
Modern aluminum processing enterprise, there is that anodic oxidation waste liquid is in need of immediate treatment, and existing processing method is excessively simple.It is first, straight
Run in and put wastewater treatment center into, both add processing cost, waste bauxite resource again, also produce substantial amounts of industrial residue；Two
It is to ask professional treatment producer to pull away.These treatment plants, if the oxidation acid pickle of single-item handling magnanimity, the alkali lye of magnanimity need to be consumed,
Society can pay the processing cost of costliness for this.
As it was previously stated, the aluminium ion in anodizing solution, optium concentration should be controlled within the scope of 3-8g/L, now obtained
Oxidation film corrosion resistance, wearability it is best, oxidation energy consumption it is low.At present, the aluminium ion concentration in anodizing tank, each enterprise are basic
Control is between 15-20g/L, far beyond optium concentration section.Aluminium ion concentration is high, and resistance is big, high energy consumption, aoxidizes film quality
Amount is poor, and these are industry common recognitions.But the environmental protection pressure of processing oxidation spent acid is limited by, enterprise is forced selection and improves aluminium ion control
The upper limit, using sacrificial oxidation film quality, increase oxidation 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：Vibrations and drift.With Al3+Exemplified by, its motion mode is：
(1), 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 shake 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 is unordered, and vibrations are eternal；
After added electric field, each ion also gradually forms in addition to drift and vibrations along the directed movement in power line direction, concentration
Gradient is distributed：
(3)、SO4 2-To anode movement after added electric field, forming anode, nearby concentration is high, and negative electrode nearby divide by the low gradient of concentration
Cloth；In anode, following electrochemical reaction is formed：
SO4 2-- 2e=2O+SO2↑ (losing electronics, release oxygen atom) (1)
2Al+3O=Al2O3(exothermic reaction, oxygenerating film) (2)
Al2O3+3H+=2Al3++3OH-(oxide-film dissolving) (3)
(4)、Al3+、H+To cathode motion after added electric field, forming negative electrode, nearby concentration is high, the low gradient of concentration near anode
Distribution；In negative electrode, following electrochemical reaction is formed：
2H++ 2e=H2↑ (obtaining electronics, discharge hydrogen) (4)
Because ionic radius is different, H+Prior to Al3+Cathode surface is reached, and because current potential is different, H+It is preferential to obtain electronics,
Al3+It can only rest in oxidation solution and constantly accumulate.From (1) (4) formula, the conductive capability at the two poles of the earth is the SO by anode4 2-
With the H at negative electrode+Concentration determine.With continuing for electrolysis, the ion constantly consumption near the two poles of the earth is, it is necessary to the SO of distal end4 2-
And H+It is continuously replenished, makes oxidation continue to carry out.At this moment, SO4 2-And H+The complexity moved 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 in oxidation solution, a certain area parallel to the two poles of the earth is A's
Section, the number at the aluminium ion vibrations center passed through is N, and each aluminum ions concussion section is S, then aluminium ion on the section
Total footprint be NS, SO4 2-And H+During by the section, it is A-NS to be influenceed less effective area by aluminium ion interception.By
This understands that aluminium ion concentration is higher, and N is bigger, and effective area A-NS is smaller, SO4 2-And H+The difficulty passed through is bigger, tank liquor resistance
It is bigger.But according to (3) formula, aluminium ion concentration is reduced, reacts and is moved to the right, oxide-film dissolving is accelerated, therefore aluminium ion concentration is not
Can be too low.Production practices prove that oxidation trough aluminium ion optium concentration is 3-8g/L, and this section film layer is optimal, and tank liquor resistance is smaller,
Energy consumption is low, and low energy consumption and high film quality, it is necessary to assure aluminium ion concentration is less than 8g/L.For that purpose it is necessary to the aluminium to oxidation trough
Ion carries out specially treated, both reduces aluminium ion, reclaims sulfur acid oxidation solution and byproduct containing aluminium again, thoroughly solves aluminium ion and surpasses
The drawbacks of a part of oxidation solution being outwelled when crossing 20g/L.
Chinese patent 201320875536.9 proposes with the method that in mould liquid and anodizing solution reclaims aluminium hydroxide is stewed, really
The aluminium hydroxide for meeting national standard GB4294-2010 requirements can be reclaimed in fact.But the method sacrifices the oxidation of this recoverable
Sulfuric acid in liquid, it is tangible unfortunate.By Chinese patent 201410126857.8,201611043945.7,201611042044.6,
201610995717.3rd, 201611038294.2,201611002760.1 method provided, can be chemically from oxidation solution
Individually crystallization aluminium ion, produces ammonium alum, and sulfuric acid all recycles.But the recovery system configuration that these patents of invention provide, no
Enough perfect, the rate of recovery is low, dosing labor intensity is high, it is impossible to meets large-scale industrial production demand.
In addition, prior art aluminium alloy anode oxide wire casing position arrangement as shown in Figure 2, is configured after 10# oxidation troughs
11#, 12# flow rinsing bowl.When aluminium is washed, bring the oxidation solution of sulfur acid, aluminium ion and ammonium ion into, add processing spent acid
With the pressure of ammonia nitrogen, the waste of medicament also result in.
Aluminium when oxidation trough is aoxidized oxidation solution temperature can rise, it is necessary to be used for using ice maker in oxidation trough
Oxidation solution cools.In the prior art, defrosted using running water to ice maker, waste a large amount of running water.
The content of the invention
It is an object of the invention to propose a kind of oxidized aluminum alloy liquid recovery and cooling device crystallization removing system, there is drop
Low environmental protection pressure, save the characteristics of water resource.
It is an object of the invention to propose that technique is removed in a kind of oxidized aluminum alloy liquid recovery and cooling device crystallization, there is labor
Fatigue resistance is low, saves the characteristics of water resource.
To use following technical scheme up to this purpose, the present invention：
A kind of oxidized aluminum alloy liquid recovery and cooling device crystallization removing system, including oxidation solution collection system, oxidation solution
Processing system, oxidation liquid separation system, washing medicament retention system and cooling device crystallization removing system；
Oxidation solution collection system includes oxidation trough, No.1 pump, retort and pipeline, and oxidation trough, No.1 pump and retort are led to
Piping is sequentially communicated, and No.1 pump is used to the oxidation solution in oxidation trough being pumped into retort；
Oxidation liquid treating system is used to add medicament into retort, makes oxidation solution and medicament mixed liquor shape in retort
Into solidliquid mixture；
Oxidation liquid separation system is used to separate the solidliquid mixture formed in oxidation liquid treating system；
Washing medicament retention system includes flowing rinsing bowl and non-mobile water washing trough, flowing rinsing bowl, non-mobile water washing trough
It is sequentially communicated with oxidation trough, flows rinsing bowl and non-mobile water washing trough is used for oxidation trough moisturizing；
Cooling device crystallization removing system includes heat exchanger and pipeline, and heat exchanger is connected by pipeline with oxidation trough
Logical, heat exchanger is used to cool to the oxidation solution in oxidation trough, and non-mobile water washing trough is connected with heat exchanger by pipeline, no
The liquid flowed in rinsing bowl enters in oxidation trough through over-heat-exchanger.
Oxidation solution is taken out of with non-mobile water washing trough retention aluminium, reclaims rear oxidation groove water shortage by oxidation solution, liquid level declines
Reaction mechanism, from flowing rinsing bowl and non-mobile water washing trough to the reverse moisturizing of oxidation trough, recovery flowing rinsing bowl and do not flow
The oxidation solution of rinsing bowl retention.Current during moisturizing reverse using non-mobile water washing trough carry out crystallization removing to heat exchanger, no
Only being capable of saving water resource, additionally it is possible to the current of moisturizing is cooled.
Further, oxidation liquid treating system includes grug feeding jar, No. two pumps and pipeline, and the top of retort is connected with circulation
Pipe, circulation pipe are connected with No. two pumps, and the inlet of grug feeding jar is connected by pipeline with circulation pipe, and retort solidliquid mixture goes out
Mouth is connected with No. two pumps, and the outlet of retort solidliquid mixture is connected with the pipeline between No. two pumps with the drug feeding pipeline of grug feeding jar
Logical, No. two pumps are used to drive the decoction in grug feeding jar to enter retort from drug feeding pipeline and circulation pipe；
Oxidation liquid separation system includes recycling can, centrifuge and pipeline, No. two pumps, recycling can and centrifuge by pipeline according to
Secondary connection, No. two pumps export with the solidliquid mixture of retort to be connected by pipeline, and No. two pumps are used for consolidating in retort
Liquid mixture is pumped into recycling can, and centrifuge is used to separate solidliquid mixture.
During dosing, the negative pressure of systemic circulation is formed by retort, No. two pumps and circulation pipe, open grug feeding jar input duct,
The partial circulating of grug feeding jar, grug feeding jar pipeline and No. two pumps, low level dosing is realized, both reduce labor intensity, prevented a high position again
The risk of operation.
Further, flowing rinsing bowl and non-mobile water washing trough has two, according to flowing rinsing bowl, flowing rinsing bowl, no
Flowing rinsing bowl, non-mobile water washing trough and oxidation trough order are sequentially communicated.Therefore, the setting of multiple groove positions can fully retain aluminium
The oxidation solution that material is taken out of when washing.
Further, oxidized aluminum alloy groove aluminium ion and retrieval of sulfuric acid and washing medicament retention system, in addition to oxidation solution
Recovery and recrystallization system, oxidation solution recovery and recrystallization system include crystallizing tank and pipeline, and the charging aperture of crystallizing tank passes through pipe
Road is connected with centrifuge, and the supernatant outlet of crystallizing tank is connected by pipeline with No. two pumps, and No. two pumps pass through pipeline and oxidation trough
Connection, the recrystallization mixture outlet of crystallizing tank are connected by pipeline with No. two pumps, and No. two pumps are used for the supernatant in crystallizing tank
Liquid pump enters oxidation trough and for the recrystallization mixture in crystallizing tank to be pumped into recycling can.
The liquid obtained through centrifuge progress separation of solid and liquid carries out recrystallization processing, the supernatant of crystallizing tank into crystallizing tank
Send oxidation trough recovery back to, the solidliquid mixture of recrystallization separates again into recycling can through centrifuge, can further improve aluminium
The rate of recovery of ion and sulfuric acid.
Further, retort is provided with least a supernatant discharge pipe, supernatant discharge pipe and is connected with crystallizing tank.
The supernatant of retort can be entered in crystallizing tank by supernatant discharge pipe., will be upper before retort discharges solidliquid mixture
Clear liquid is discharged into crystallizing tank, can reduce separation of solid and liquid total amount, system is more suitable for large-scale industrial production demand.
Further, electric agitator is provided with retort, recycling can, crystallizing tank and grug feeding jar, in order to in tank
Material is stirred.
A kind of technique for crystallizing removing system with cooling device using the recovery of above-mentioned oxidized aluminum alloy liquid, including following step
Suddenly：
(1) oxidation solution is collected：Oxidation solution in oxidation trough is pumped into retort by No.1 pump, and the oxidation solution in retort reaches
During predetermined amount, No.1 pump is closed；
(2) oxidation solution is handled：No. two pumps are opened, the oxidation solution in retort is followed in retort, No. two pumps, circulation pipes
Circulation moves, and the logical inlet from grug feeding jar of partial oxidation liquid enters in grug feeding jar, and medicament is added in grug feeding jar, in grug feeding jar
Decoction driven and enter in circulation pipe by No. two pumps by drug feeding pipeline, afterwards into retort, additive amount of medicament reaches pre-
If during amount, stop dosing, close the mixed liquor standing of No. two pumps, retort internal oxidition liquid and medicament, form solidliquid mixture；
(3) oxidation solution separates：Solidliquid mixture in retort is pumped into recycling can by No. two pumps, opens centrifuge, separation
Solidliquid mixture is recovered liquid and crystalline product, and recovered liquid is delivered into crystallizing tank recrystallization；
(4) oxidation solution reclaims：Supernatant in crystallizing tank is recycled to oxidation trough through No. two pumps；
(5) recrystallization recovery：Recrystallization mixture in crystallizing tank is pumped into recycling can by No. two pumps, is carried out solid-liquid again and is mixed
Compound separates；
(6) medicament retention is washed：Liquid in flowing rinsing bowl enters non-mobile water washing trough, the liquid of non-mobile water washing trough
Into oxidation trough, to oxidation trough moisturizing, the medicament of recovery non-mobile water washing trough retention；
(7) cooling device crystallization is removed：Liquid in non-mobile water washing trough enters oxidation trough through heat exchanger, cleans heat and hands over
Parallel operation, remove the crystallization on heat exchanger.
Using above-mentioned recovery process, the rate of recovery can not only be improved, also achieves low level dosing, it is strong both to have reduced work
Degree, has prevented the risk of high-order homework again.Also, oxidation trough watering step can reclaim flowing rinsing bowl and non-mobile water washing trough is cut
The oxidation solution stayed, reduce the environmental protection pressure of wastewater treatment, moreover it is possible to reclaim oxidation solution.During moisturizing reverse using non-mobile water washing trough
Current carry out crystallization removing to heat exchanger, can not only saving water resource, additionally it is possible to the current of moisturizing is cooled.
Further, the medicament in grug feeding jar is ammonium sulfate, when ammonium sulfate addition reach in oxidation solution aluminium to be cleaned from
During son 2.45 times of weight of amount, stop dosing.It can ensure that the aluminium ion in oxidation solution can be filled by accurate calculation chemical feeding quantity
Distinguish and remove, the excessive quality for influenceing recovered liquid of chemical feeding quantity can be prevented again.
Further, in step, (in (3), the solidliquid mixture in retort is pumped into before recycling can, in retort
The supernatant in portion is discharged into crystallizing tank.So as to reduce the total amount of separation of solid and liquid.
Further, it is provided with electric agitator in retort, recycling can, crystallizing tank and grug feeding jar；In adding for step (2)
During medicine, the electric agitator in retort and grug feeding jar is opened；In step (3), the electric agitator in recycling can is opened,
In step (5), the electric agitator in crystallizing tank is opened.
Beneficial effects of the present invention are：
1st, the present invention crystallizes again using in retort primary crystal, recycling can separation and crystallizing tank, can fully reclaim
Aluminium ion and sulfuric acid in oxidation solution, the rate of recovery are high；
2nd, oxidation trough connects with retort, and crystallizing tank connects with oxidation trough, can realize that oxidation solution is handled online, aluminium ion
It does not interfere with each other, can carries out simultaneously with retrieval of sulfuric acid and aluminum alloy surface processing；
3rd, low level dosing is realized using negative pressure during No. two pump works, grug feeding jar Automatic Dosing, it is strong has both reduced work
Degree, has prevented the risk of high-order homework again；
4th, the rate of recovery proposes high-low position dosing and supernatant discharge pipe, the setting of overflow pipe so that system of the invention and
Technique more sprouts purchase and meets large-scale industrial production demand；
5th, using washing medicament retention system, take oxidation solution out of with non-mobile water washing trough retention aluminium, returned by oxidation solution
Receive rear oxidation groove water shortage, the reaction mechanism that liquid level declines, from flowing rinsing bowl and non-mobile water washing trough to the reverse moisturizing of oxidation trough,
Recovery flowing rinsing bowl and the oxidation solution of non-mobile water washing trough retention, it can not only reduce the environmental protection pressure of wastewater treatment, moreover it is possible to
Reclaim oxidation solution；
6th, current during moisturizing reverse using non-mobile water washing trough carry out crystallization removing to heat exchanger, can not only save
Water resource, additionally it is possible to make the current of moisturizing cool.
Brief description of the drawings
Fig. 1 is that the oxidized aluminum alloy liquid recovery of one embodiment of the invention and the structure of cooling device crystallization removing system are shown
It is intended to；
Fig. 2 is aluminium alloy anode oxide wire casing position layout drawing in the prior art；
Fig. 3 is the structural representation for the retrieval of sulfuric acid machine that prior art oxidation trough is equipped with.
Wherein：Oxidation trough 1, No.1 pump 2, retort 3, overflow pipe 31, No. two pumps 4, recycling can 5, centrifuge 6, crystallizing tanks
7th, grug feeding jar 8, drug feeding pipeline 81, the feed tube 82 of grug feeding jar, flowing rinsing bowl 9, non-mobile water washing trough 10, heat exchanger 11, one
Number valve of valve 08, nine of valve 07, eight of valve 06, seven of valve 05, six of valve 04, five of valve 03, four of valve 02, three of valve 01, two
09th, No. ten valves 010, the valve 015,16 of valve 014,15 of valve 013,14 of valve 012,13 of ride on Bus No. 11 valve 011,12
Number valve 019,20 of valve 018,19 of valve 017,18 of valve 016,17 valve 020, two ride on Bus No. 11 valves 021,22
Number valve 024 of valve 023,24 of valve 022,23；
Oxidation trough 100, retrieval of sulfuric acid machine 101, permeable membrane 102, pump 103.
Embodiment
Below in conjunction with the accompanying drawings and embodiment further illustrates technical scheme.
First, the theoretical foundation of aluminium ion and retrieval of sulfuric acid in anodizing solution
During oxidized aluminum alloy, by (3) formula, partial oxide film is dissolved, and about 4Kg/T (400m2) aluminium dissolves 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↓ (5)
Under conditions of 160-200g/L sulfuric acid, containing aluminium and ammonium ion, alum NH4Al(SO4)2·12H2O crystallization analysis
Go out, the number of aluminium residual is relevant with crystallization temperature and time.
2nd, quantitative analytical experiment result
Take 1 liter of anodizing solution, free sulfuric acid 183.9g/L, Al3+20.20g/L, electrical conductivity 152.5s/m, 25 DEG C of temperature,
Addition ammonium sulfate is tested.After crystallization 20 minutes, sulfuric acid concentration, aluminium ion concentration and the electrical conductivity of tank liquor, knot are measured immediately
Fruit is as shown in table 1：
The bath parameters of table 1 with various concentrations ammonium sulfate changing rule
By (5) formula, 1g/L Al are often crystallized3+, it is necessary to 2.45g/L ammonium sulfate is added, 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：
1st, ammonium sulfate is added in oxidation solution, under normal temperature, crystallizable precipitation alum in the short time；
2nd, as the increase of ammonium sulfate addition, aluminium ion gradually reduce, but the range of decrease narrows；
3rd, as crystallization time increases, aluminium ion further reduces；
4th, solubility of the alum at 30 DEG C is 170g/L in oxidation solution, and solubility at 20 DEG C is 150g/L, 10
DEG C when solubility be 130g/L, as crystallization temperature reduces, aluminium ion concentration reduce；Even if ammonium ion excess, low temperature and length
Time crystallizes, and aluminium ion can not be fully crystallized precipitation；
Even if the 5, ammonium ion is excessive, low temperature and long-time crystallize, aluminium ion can not be fully crystallized precipitation；
6th, with the increase of ammonium sulfate addition, sulfuric acid concentration increase；
7th, with the increase of ammonium sulfate addition, electrical conductivity increase.
3rd, aluminium alloy anode oxide groove aluminium ion and retrieval of sulfuric acid Process configuration
It is actual with reference to oxidation line quantity-produced according to the experimental result of reaction equation (5) and table 1, sulfuric acid and washing medicament
When retention recovery, the collection of byproduct, because the solubility of ammonium vanadium is very sensitive to temperature, when the temperature of oxidation solution is 20 DEG C,
Ammonium vanadium solubility is 150g/L, and the temperature at heat exchanger (ice maker or plate heat exchanger) heat exchange is less than 5 DEG C, and ammonium vanadium dissolves
Degree is less than 100g/L.When working long hours, it is easy to crystallize at heat exchanger heat exchange, influences heat exchanger effectiveness, may when serious
Cause to stop production, it is necessary to the method that crystallization is removed in design.Alumilite process liquid reclaims to be set with cooling device crystallization removing system by Fig. 1
Meter.
This recovery system is by the aluminum oxide profile design for producing 100000 tons per year.Produce 100000 tons of aluminium section bars per year, produce 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 accompanying drawing3Oxidation waste liquid retort, 1
40M3Oxidation solution recycling can, 1 40M3Oxidation solution crystallizing tank, 1 10M3Grug feeding jar, a desk centrifuge, and supporting pipeline,
Pump and valve.
The characteristics of being not easy long-distance pipeline in view of oxidation solution, the system should set individually oxidation liquid waste processing area
Domain, it is convenient that oxidation solution after processing is directly returned into oxidation trough with pipeline close to oxidation workshop.
Tank, pump, valve and the pipeline contacted with oxidation waste liquid, it is necessary to by acidproof design, it is contemplated that oxidation waste liquid does not decompose, no
Pipeline and valve are blocked, from acid-proof pump, from oxidation trough stringing and valve, oxidation waste liquid is evacuated to retort, adopted in retort
Stirred with motor.
Oxidized aluminum alloy liquid reclaims and cooling device crystallization removing system, including the processing of oxidation solution collection system, oxidation solution
System oxidation liquid separation system, oxidation solution recovery and recrystallization system, washing medicament retention system and cooling device crystallization are removed
System.
Oxidation solution collection system includes oxidation trough 1, No.1 pump 2, retort 3 and pipeline, oxidation trough 1, No.1 pump 2 and reaction
Tank 3 is sequentially communicated by pipeline, and No.1 pump 2 is used to the oxidation solution in oxidation trough 1 being pumped into retort 3, and oxidation solution is reacting
Solidliquid mixture is formed in tank 3.No.1 valve 01 is provided between oxidation trough 1 and No.1 pump 2.The bottom of retort 3 is provided with solid
Liquid mixture exports, and sets No. ten valves 010 in the exit.Electric agitator is provided with retort 3, in order to retort
Oxidation solution in 3 is stirred, and the medicament of addition can be made to be well mixed with oxidation solution.
Oxidation liquid treating system includes grug feeding jar 8, No. two pumps 4 and pipelines.The top of retort 3 is connected with circulation pipe 32,
Circulation pipe 32 connects with No. two pumps 4.The one end for the pipeline that No. two pumps 4 are connected with oxidation trough 1 connects with oxidation trough 1, the other end
It is connected by three-way pipe with circulation pipe 32, the pipeline structure of system can be simplified.Seven are provided between three-way pipe and No. two pumps 4
Number valve 07.
The inlet of grug feeding jar 8 is connected by pipeline with circulation pipe 32, connectivity part be located at No. seven valves 07 and No. two pumps 4 it
Between., ten No. two valves 012 are provided with the pipeline.The solidliquid mixture of retort 3 exports the pipeline and dosing between No. two pumps 4
The drug feeding pipeline 81 of tank 8 is connected, pipeline of the connectivity part between No. six valves 06 and No. two pumps 4.No. two pumps 4 are used to drive
Decoction in grug feeding jar 8 enters retort 3 from drug feeding pipeline 81 and circulation pipe 32.
During dosing, the negative pressure of systemic circulation is formed by 3, No. two pumps 4 of retort and circulation pipe 32, opens grug feeding jar feed tube
Road 82, grug feeding jar 8, the partial circulating of grug feeding jar pipeline 81 and No. two pumps 4, realize low level dosing, both reduce labor intensity, shut out again
The risk of high-order homework absolutely.
Oxidation liquid separation system includes recycling can 5, centrifuge 6 and pipeline, and No. two pumps 4, recycling can 5 and centrifuge 6 pass through
Pipeline is sequentially communicated, and No. two pumps 4 export with the solidliquid mixture of retort 3 to be connected by pipeline, and No. two pumps 4 are used for will reaction
Solidliquid mixture in tank 3 is pumped into recycling can 5, and centrifuge 6 is used to separate solidliquid mixture.The entrance of recycling can 5 is provided with
Ten No. six valves 016, exit are provided with ten No. seven valves 017.Electric agitator is provided with recycling can 5, in order in recycling can 5
Solidliquid mixture smoothly enters centrifuge 6.
The top of retort 3 is provided with overflow pipe 31, and overflow pipe 31 is connected with crystallizing tank 7.When liquid is excessive in retort 3
When, crystallizing tank 7 can be entered by overflow pipe 31, prevent from leaking, system is more suitable for large-scale industrial production demand.
Oxidation solution reclaims and recrystallization system includes crystallizing tank 7 and pipeline.The charging aperture of crystallizing tank 7 passes through pipeline and centrifugation
Machine 6 connects.The supernatant outlet of crystallizing tank 7 is connected by pipeline with No. two pumps 4, and No. two pumps 4 are connected by pipeline and oxidation trough 1
Logical, the recrystallization mixture outlet of crystallizing tank 7 is connected by pipeline with No. two pumps 4, and No. two pumps 4 are for by crystallizing tank 7
Clear liquid is pumped into oxidation trough 1 and for the recrystallization mixture in crystallizing tank 7 to be pumped into recycling can 5.Crystallizing tank 7 is provided with electricity and stirred
Device is mixed, in order to which the recrystallization mixture in crystallizing tank 7 smoothly enters in recycling can 5.
Retort 3 is provided with supernatant discharge pipe, and supernatant discharge pipe is connected with crystallizing tank 7.The supernatant of retort 3
It can be entered by supernatant discharge pipe in crystallizing tank 7.Before retort 3 discharges solidliquid mixture, supernatant is discharged into crystallization
In tank 7, separation of solid and liquid total amount can be reduced.
In present embodiment, supernatant discharge pipe has two, the different height being separately positioned in retort 3, keeps up with more
Clear liquid discharge pipe is connected with the different height on crystallizing tank 7 respectively, and two supernatant discharge pipes are connected with No. two pumps 4.It is more
Root supernatant discharge pipe is set in different height, the supernatant discharge pipe on proper height can be selected according to actual conditions, also
More supernatant discharge pipes can be selected simultaneously, are increased the supernatant velocity of discharge, system is more suitable for large-scale industrial production
Demand.
In other embodiments, supernatant discharge pipe can be one or more than two.
The supernatant outlet of crystallizing tank 7 is connected with supernatant discharge pipe.Two supernatant discharge pipes are at retort 3
It is respectively arranged with No. two valves 02 and No. three valves 03.Two supernatant discharge pipes are respectively arranged with No. four valves 04 at crystallizing tank 7
With No. five valves 05.Ride on Bus No. 11 valve 011 is provided with the recrystallization mixture outlet of crystallizing tank 7.
Pipeline, the crystallizing tank 7 of the solidliquid mixture of retort 3 outlet recrystallize mixture outlet pipeline and No. two pumps 4 with
The pipeline of supernatant connection is connected by four-way pipe.No. six valves 06 are provided between No. two pumps 4 and four-way pipe.No. two pumps 4 and oxygen
Change and be provided with No. nine valves 09 on the pipeline that groove 1 is connected, the pipeline structure of system can be simplified.
Washing medicament retention system includes flowing rinsing bowl 9 and non-mobile water washing trough 10, flowing rinsing bowl 9, non-mobile water
Washing trough 10 and oxidation trough 1 are sequentially communicated, and flow rinsing bowl 9 and non-mobile water washing trough 10 is used for the moisturizing of oxidation trough 1.
In present embodiment, flowing rinsing bowl 9 and non-mobile water washing trough 10 has two, according to flowing rinsing bowl 9, flowing
Rinsing bowl 9, non-mobile water washing trough 10, non-mobile water washing trough 10 and the order of oxidation trough 1 are sequentially communicated.And flow rinsing bowl 9, no
Flowing rinsing bowl 10, non-mobile water washing trough 10 and oxidation trough 1 it is bright between be respectively arranged with two No. ten valves, 020, ten No. nine valve
019 and ten No. eight valve 018.Flowing rinsing bowl 9 close to non-mobile water washing trough 10 is provided with outlet pipe, and water outlet pipe part is provided with two
Ride on Bus No. 11 valve 021.Another flowing rinsing bowl 9 is provided with water inlet pipe.
Cooling device crystallization removing system includes heat exchanger 11 and pipeline, and heat exchanger 11 passes through pipeline and oxidation trough 1
It is connected, heat exchanger 11 is used to cool to the oxidation solution in oxidation trough 1, and non-mobile water washing trough 10 passes through pipe with heat exchanger 11
Road is connected, and the liquid in non-mobile water washing trough 10 enters in oxidation trough 1 through over-heat-exchanger 11.The import of heat exchanger 11 with
20 No. two valves 022, the pipe between the import of heat exchanger 11 and oxidation trough 1 are provided with pipeline between non-mobile water washing trough
20 No. three valves 023 are provided with road, 20 No. four valves are provided with the pipeline between the outlet of heat exchanger 11 and oxidation trough 1
024。
Rely on said system to set, the oxidation waste liquid of aluminum fabrication plant magnanimity is delivered to retort, by 2.45 times of aluminium ions
Strength by weight adds ammonium sulfate, and crystallization separates out alum, realizes that sulfuric acid oxidation liquid reclaims completely, and reclaim substantial amounts of aluminum sulfate
Ammonium byproduct.Oxidized aluminum alloy liquid reclaims removes technique with cooling device crystallization, comprises the following steps：
(1) oxidation solution is collected：Oxidation solution in oxidation trough 1 is pumped into retort 3 by No.1 pump 2, the oxidation solution in retort 3
When reaching predetermined amount, No.1 pump 2 is closed；
(2) oxidation solution is handled：No. two pumps 4 are opened, make the oxidation solution in retort 3 in retort 3, No. two pumps 4, circulation pipes
Circulated in 32, the logical inlet from grug feeding jar 8 of partial oxidation liquid enters in grug feeding jar 8, and adds medicine in grug feeding jar 8
Agent, the decoction in grug feeding jar 8 is driven into circulation pipe 32 by drug feeding pipeline 81 by No. two pumps 4, afterwards into retort 3
In, when additive amount of medicament reaches predetermined amount, stop dosing, close the mixed liquor of No. two pumps 4, the internal oxidition liquid of retort 3 and medicament
Stand, form solidliquid mixture；
(3)) oxidation solution separates：Solidliquid mixture in retort 3 is pumped into recycling can 5 by No. two pumps 4, opens centrifuge,
It is recovered liquid and crystalline product to separate solidliquid mixture, and recovered liquid is delivered into crystallizing tank 7 recrystallizes；
(4) oxidation solution reclaims：Supernatant in crystallizing tank 7 is recycled to oxidation trough 1 through No. two pumps 4；
(5) recrystallization recovery：Recrystallization mixture in crystallizing tank 7 is pumped into recycling can 5 by No. two pumps 7, is consolidated again
Liquid mixture separates；
(6) oxidation trough moisturizing：Liquid in flowing rinsing bowl 9 enters non-mobile water washing trough 10, non-mobile water washing trough 10
Liquid enters oxidation trough 1, to the moisturizing of oxidation trough 1, the medicament of the retention of recovery non-mobile water washing trough 10；
(7) cooling device crystallization is removed：Liquid in non-mobile water washing trough enters oxidation trough through heat exchanger, cleans heat and hands over
Parallel operation, remove the crystallization on heat exchanger.
Further, the medicament in grug feeding jar is ammonium sulfate, when ammonium sulfate addition reach in oxidation solution aluminium to be cleaned from
During son 2.45 times of weight of amount, stop dosing.It can ensure that the aluminium ion in oxidation solution can be filled by accurate calculation chemical feeding quantity
Distinguish and remove, the excessive quality for influenceing recovered liquid of chemical feeding quantity can be prevented again.
Further, in step (3), the solidliquid mixture in retort 3 is pumped into before recycling can 5, by retort 3
The supernatant on top is discharged into crystallizing tank 7.So as to reduce the total amount of separation of solid and liquid.
Further, it is provided with electric agitator in retort 3, recycling can 5, crystallizing tank 7 and grug feeding jar 8；In step (2)
Dosing during, open the electric agitator in retort 3 and grug feeding jar 8；In step (3), the electricity opened in recycling can 5 stirs
Device is mixed, in step (5), opens the electric agitator in crystallizing tank 7.
Specific technological process is as follows：
1st, oxidation solution is collected：No.1 valve 01 is opened, closes 02, No. three valve 03 of No. two valves and No. ten valves 010, opens No.1 pump
2, the pending oxidation solution in oxidation trough 1 is pumped into 15cm under retort 3 to overfall, the pending oxidation solution of collection is completed and enters instead
Answer tank flow；
2nd, oxidation solution is handled：No. two valve 03, nine of valve 02, three valves 09, ride on Bus No. 11 valve 011 and ten No. four valves 014 are closed,
Open the electric agitator in retort 3；No. six valves 08 of valve 07, eight of valve 06, seven and No. ten valves 010 are opened, open No. two pumps
4, circulate pending oxidation solution；Under conditions of the pending oxidation solution of systemic circulation is kept, ten No. two valves 012 are opened, to grug feeding jar
Add 7 plus pending oxidation solution；Open the electric agitator that grug feeding jar 8 adds, addition ammonium sulfate to grug feeding jar 8；Open ten No. three valves
013, the partial circulating of grug feeding jar 8 is opened, ammonium ion oxidation solution will be contained and be pumped into retort 3；When ammonium sulfate addition reaches to be cleaned
During 2.45 times of weight of aluminium ion amount, stop dosing；Electric agitator in retort 3 continues stirring 30 minutes, complete to ammonium sulfate
Dissolving, stop stirring；Precipitation, 60 minutes are stood, the oxidation solution in retort 3 is changed into solid-liquid with ammonium sulfate mixed liquor and mixed
Thing, complete pending oxidation solution chemical treatment flow；
3rd, oxidation solution separates：Open 02, No. four valve 04 of No. two valves or open 03, No. five valve 05 of No. three valves, by retort 3
In supernatant be put into crystallizing tank 7, reduce separation of solid and liquid total amount；07, ten No. five valve 015 of No. seven valves and ten No. seven valves 017 are closed,
No. ten valves 014 of valve 06,14 of valve 010, six and ten No. six valves 016 are opened, No. two pumps 4 are opened, by the solid-liquid in retort 3
Mixture is pumped into recycling can 5；Open the electric agitator and centrifuge 6 in recycling can 5；Open ten No. seven valves 017, separation of solid and liquid ammonium
Vanadium, and recovered liquid is delivered to crystallizing tank 7 and recrystallized, complete oxidation liquid separation system operating process；
4th, oxidation solution reclaims：Close 08, No. ten valve 010 of No. two valves of valve 03, eight of valve 02, three, ride on Bus No. 11 valve 011 and ten
No. four valves 014,06, No. seven valve 07 of No. six valves and No. nine valves 09 are opened, open No. four valves 04 or No. five valves 05, open No. two pumps 4,
Send the supernatant in crystallizing tank 7 back to oxidation trough 1, complete oxidation solution reclaimer operation flow；
5th, the recovery of ammonium vanadium is recrystallized：Close No. two valves 07, ten of valve 05, seven of valve 04, five of valve 03, four of valve 02, three
Number valve 010,011, ten No. three valve 013 of ride on Bus No. 11 valve and ten No. five valves 015, the electric agitator in crystallizing tank 7 is opened, open 11
Number valve 014 of valve 06,14 of valve 011, six and ten No. six valves 016, recrystallization mixture is pumped into recycling can 5, repeats solid-liquid
Lock out operation flow, complete recrystallization ammonium vanadium reclaimer operation flow.
6th, rinsing bowl medicament retains：Ten No. eight valves, 018, ten No. nine valve 019 and two No. ten valves 020 are opened, close 21
Number valve 021, current flow to oxidation trough by flowing rinsing bowl 9, flowing rinsing bowl 9, non-mobile water washing trough 10, non-mobile water washing trough 10
1 flowing, reverse moisturizing.The oxidation solution that two non-mobile water washing troughs 10 of recovery retain, the oxidation solution is by aluminium autoxidation groove band
Go out, complete the retention of rinsing bowl medicament and reclaimer operation flow.
7th, cooling device crystallization is removed：20 No. three valves 023, two ride on Bus No. 11 valves, 021, ten No. eight valve 018 are closed, opens ten
No. nine valves 022 of valve 020,22 of valve 019,20 and 20 No. four valves 024, heat exchanger 11 is opened, current are by flowing
Rinsing bowl 9, non-mobile water washing trough 10, through heat exchanger 11 oxidation trough 1 is flowed to, to 1 reverse moisturizing of oxidation trough.Reclaim non-mobile water
The oxidation solution of washing trough retention, cleans heat exchanger 11, completes cooling device crystallization and removes.
Aluminium ion crystallization separates out, oxidation solution recycles, and has avoided the huge of sulfuric acid caused by outwelling oxidation solution and bauxite resource
It is big to waste, reduce 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
Reduce.In table 1, Al3+During 20.20g/L, electrical conductivity 152.5s/m；Al3+During 9.00g/L, electrical conductivity 164.25s/m.Electrical conductivity
Increase by 7.7%, i.e. oxidation solution resistance reduce by 7.7%.Aluminium processing enterprise, one ton of aluminium is aoxidized, consume about 1000 degree of electricity, reduce
7.7% resistance, it is meant that less with 77 degree of electricity；In view of electric current by when, tank liquor resistance makes tank liquor heat up, and also needs heat exchanger
Cooling power consumption, crystallization aluminium ion, reduce tank liquor resistance, reduce cooling energy consumption, energy-saving index can further improve.
The present invention crystallizes again using in retort primary crystal, recycling can separation and crystallizing tank, can fully reclaim oxygen
Change the aluminium ion and sulfuric acid in liquid, the rate of recovery is high.The aluminum ions rate of recovery is up to 90%.Oxidation trough connects with retort, crystallization
Tank is connected with oxidation trough, can realize that oxidation solution is handled online, and aluminium ion and retrieval of sulfuric acid are not done mutually with aluminum alloy surface processing
Disturb, can carry out simultaneously；Using negative pressure during No. two pump works, grug feeding jar Automatic Dosing realizes low level dosing, has both reduced work
Intensity, the risk of high-order homework is prevented again；The rate of recovery proposes high-low position dosing and supernatant discharge pipe, the setting of overflow pipe,
So that the system and technique of the present invention more sprout purchase and meet large-scale industrial production demand；The pipe-line system structure letter of the present invention
It is single, it is easy to, in Facility Layout, save floor occupying area.
The present invention further utilizes non-mobile water washing trough, the oxidation solution that retention aluminium is taken out of, is not only able to because ammonium vanadium returns
The oxidation trough that liquid level declines after receipts oxidation solution carries out moisturizing, additionally it is possible to further reclaims oxidation solution, reduces the environmental protection of wastewater treatment
Pressure.
The present invention further using the current cleaning heat exchanger 11 during reverse moisturizing, completes cooling device crystallization and removed,
Saving water resource.
The technical principle of the present invention is described above in association with specific embodiment.These descriptions are intended merely to explain the present invention's
Principle, and limiting the scope of the invention can not be construed in any way.Based on explanation herein, the technology of this area
Personnel would not require any inventive effort the other embodiments that can associate the present invention, and these modes are fallen within
Within protection scope of the present invention.
Claims (10)
1. a kind of oxidized aluminum alloy liquid recovery and cooling device crystallization removing system, it is characterised in that collect system including oxidation solution
System, oxidation liquid treating system, oxidation liquid separation system, washing medicament retention system and cooling device crystallization removing system；
The oxidation solution collection system includes oxidation trough, No.1 pump, retort and pipeline, the oxidation trough, No.1 pump and reaction
Tank is sequentially communicated by pipeline, and the No.1 pump is used to the oxidation solution in oxidation trough being pumped into retort；
The oxidation liquid treating system is used to add medicament into retort, makes oxidation solution and medicament mixed liquor shape in retort
Into solidliquid mixture；
The oxidation liquid separation system is used to separate the solidliquid mixture formed in oxidation liquid treating system；
The washing medicament retention system includes flowing rinsing bowl and non-mobile water washing trough, the flowing rinsing bowl, non-mobile water
Washing trough and oxidation trough are sequentially communicated, and the flowing rinsing bowl and non-mobile water washing trough are used for oxidation trough moisturizing；
The cooling device crystallization removing system includes heat exchanger and pipeline, and the heat exchanger passes through pipeline and oxidation trough phase
Connection, the heat exchanger are used to cool to the oxidation solution in oxidation trough, and the non-mobile water washing trough passes through pipe with heat exchanger
Road is connected, and the liquid in the non-mobile water washing trough enters in oxidation trough through over-heat-exchanger.
2. oxidized aluminum alloy liquid recovery according to claim 1 and cooling device crystallization removing system, it is characterised in that institute
Stating oxidation liquid treating system includes grug feeding jar, No. two pumps and pipeline, and the top of the retort is connected with circulation pipe, the circulation
Pipe is connected with No. two pumps, and the inlet of the grug feeding jar is connected by pipeline with circulation pipe, the retort solidliquid mixture
Outlet is connected with No. two pumps, the chemical feed pipe of pipeline and grug feeding jar between the retort solidliquid mixture outlet and No. two pumps
Road is connected, and No. two pumps are used to drive the decoction in grug feeding jar to enter retort from drug feeding pipeline and circulation pipe；
The oxidation liquid separation system includes recycling can, centrifuge and pipeline, and No. two pumps, recycling can and the centrifuge pass through pipe
Road is sequentially communicated, and No. two pumps export with the solidliquid mixture of retort to be connected by pipeline, and No. two pumps are used for will
Solidliquid mixture in retort is pumped into recycling can, and the centrifuge is used to separate solidliquid mixture.
3. oxidized aluminum alloy liquid recovery according to claim 1 and cooling device crystallization removing system, it is characterised in that institute
Stating flowing rinsing bowl and non-mobile water washing trough has two, according to flowing rinsing bowl, flowing rinsing bowl, non-mobile water washing trough, no
Flowing rinsing bowl and oxidation trough order are sequentially communicated.
4. oxidized aluminum alloy liquid recovery according to claim 2 and cooling device crystallization removing system, it is characterised in that also
System is reclaimed and recrystallized including oxidation solution, and the oxidation solution recovery and recrystallization system include crystallizing tank and pipeline, the knot
The charging aperture of brilliant tank is connected by pipeline with centrifuge, and the supernatant outlet of the crystallizing tank is connected by pipeline with No. two pumps,
No. two pumps are connected by pipeline with oxidation trough, and the recrystallization mixture outlet of the crystallizing tank is connected by pipeline and No. two pumps
Logical, No. two pumps are used to the supernatant in crystallizing tank being pumped into oxidation trough and for by the recrystallization mixture in crystallizing tank
It is pumped into recycling can.
5. oxidized aluminum alloy liquid recovery according to claim 4 and cooling device crystallization removing system, it is characterised in that institute
State retort and be provided with an at least supernatant discharge pipe, the supernatant discharge pipe is connected with crystallizing tank.
6. oxidized aluminum alloy liquid recovery according to claim 4 and cooling device crystallization removing system, it is characterised in that institute
State and electric agitator is provided with retort, recycling can, crystallizing tank and grug feeding jar.
7. a kind of technique for crystallizing removing system with cooling device using oxidized aluminum alloy liquid recovery described in claim 4, it is special
Sign is, comprises the following steps：
(1) oxidation solution is collected：Oxidation solution in oxidation trough is pumped into retort by the No.1 pump, the oxidation solution in the retort
When reaching predetermined amount, No.1 pump is closed；
(2) oxidation solution is handled：No. two pumps are opened, make the oxidation solution in the retort in retort, No. two pumps, circulation pipes
In circulate, the logical inlet from grug feeding jar of partial oxidation liquid enters in grug feeding jar, and medicament is added in grug feeding jar, described
Decoction in grug feeding jar is driven by drug feeding pipeline by No. two pumps to be entered in circulation pipe, afterwards into retort, medicament addition
When amount reaches predetermined amount, stop dosing, close No. two pumps, the mixed liquor of the retort internal oxidition liquid and medicament stands, formed
Solidliquid mixture；
(3) oxidation solution separates：Solidliquid mixture in retort is pumped into recycling can by No. two pumps, opens centrifuge, separation
Solidliquid mixture is recovered liquid and crystalline product, and recovered liquid is delivered into crystallizing tank recrystallization；
(4) oxidation solution reclaims：Supernatant in the crystallizing tank is recycled to oxidation trough through No. two pumps；
(5) recrystallization recovery：Recrystallization mixture in crystallizing tank is pumped into recycling can by No. two pumps, is carried out solid-liquid again and is mixed
Compound separates；
(6) medicament retention is washed：Liquid in the flowing rinsing bowl enters non-mobile water washing trough, the liquid of non-mobile water washing trough
Into oxidation trough, to oxidation trough moisturizing, the medicament of recovery non-mobile water washing trough retention；
(7) cooling device crystallization is removed：Liquid in the non-mobile water washing trough enters oxidation trough through heat exchanger, cleans heat and hands over
Parallel operation, remove the crystallization on heat exchanger.
8. the recovery of oxidized aluminum alloy liquid and the technique of cooling device crystallization removing system, its feature exist according to claim 7
In the medicament in the grug feeding jar is ammonium sulfate, when ammonium sulfate addition reaches 2.45 times of aluminium ion amount to be cleaned in oxidation solution
During weight, stop dosing.
9. the recovery of oxidized aluminum alloy liquid and the technique of cooling device crystallization removing system, its feature exist according to claim 7
In in the step (3), the solidliquid mixture in retort is pumped into before recycling can, by the supernatant of retort internal upper part
It is discharged into crystallizing tank.
10. the recovery of oxidized aluminum alloy liquid and the technique of cooling device crystallization removing system, its feature exist according to claim 7
In being provided with electric agitator in the retort, recycling can, crystallizing tank and grug feeding jar；During the dosing of step (2),
Open the electric agitator in retort and grug feeding jar；In step (3), the electric agitator in recycling can is opened, in step (5)
In, open the electric agitator in crystallizing tank.
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| CN107858731B (en) | 2019-10-01 |
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