CN104451166B - The method and apparatus of zinc and chromium in a kind of recycling heavy metal sewage sludge - Google Patents
The method and apparatus of zinc and chromium in a kind of recycling heavy metal sewage sludge Download PDFInfo
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- CN104451166B CN104451166B CN201410855721.0A CN201410855721A CN104451166B CN 104451166 B CN104451166 B CN 104451166B CN 201410855721 A CN201410855721 A CN 201410855721A CN 104451166 B CN104451166 B CN 104451166B
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Abstract
The present invention provides a kind of method and apparatus for recycling zinc and chromium in heavy metal sewage sludge, and the method for zinc and chromium in recycling heavy metal sewage sludge, is to comprise the steps of: pretreatment leaching, is neutralized, evaporates and is electrolysed；Recycle the device of zinc and chromium in heavy metal sewage sludge, including multilevel leaching system, acid-base neutralization system, evaporation and crystallization system, electrolysis system and medicine system；Zinc and chromium in heavy metal sewage sludge can be successfully separated using the technique and device that propose in the present invention, realize waste resource recovery, the rate of recovery of zinc and chromium is respectively greater than 95% and 90%；The product income of acquisition is greater than operating cost, has practical application value.
Description
Technical field
The invention belongs to municipal solid wastes disposal and recycling field, in particular to zinc in a kind of recycling heavy metal sewage sludge
With the method and apparatus of chromium.
Background technique
Heavy metal sewage sludge is many kinds of.In China, the main source industry containing solid waste of heavy metal is attached most importance to non-ferrous metal ore mining
The big industry of choosing, smelting, lead storage battery, leather and leather products, chemical raw material and its product etc. five, and often belong to hazardous waste.
By 2007, be included in the leaded of " National Hazard waste register ", mercury, pot, chromium, arsenic hazardous waste yield be 1690.55
Ten thousand tons；Metal product industry, leather and leather products industry, non-ferrous metal metallurgy and calendering processing industry, chemical raw material and chemicals system
It makes industry and nonferrous metals ore picks up five discharge amounts of the industry containing heavy metal waste such as industry and accounts for whole industrial total releases
95.24%.Heavy metal sewage sludge will cause the serious pollution of soil and water body if just discharging without processing, and heavy metal is logical
The enrichment of food link layer layer is crossed, chronic/cumulative toxicity is generated, human health and bio-diversity is caused to seriously endanger.
In many industrial solid wastes, content of beary metal is relatively high, the content of many heavy metals already exceed its
Grade in metallic ore.Heavy metal in heavy metal sewage sludge is recycled, waste resource recovery utilization not only may be implemented, moreover it is possible to
It is to kill two birds with one stone that waste toxicity, which is reduced, to reduce disposal costs.The comprehensive utilization technique of heavy metal waste include dry method and
Wet process two major classes, and for recycling elemental chromium and zinc or wet process it is more.Hydrometallurgic recovery technology mainly include leach and
Separation.The most common wet recycling process has acidleach and ammonia leaching.The leaching rate of acidic leaching method is very high, but selectivity is not strong；Ammonia
Leaching method is stronger to the selectivity of copper, nickel, cobalt, less to the recycle of other metals.Later separation method after leaching has extraction
It follows the example of and chemical precipitation method.Using suitable extraction separation method, the rate of recovery of metal target is very high, and the metallic salt obtained produces
The purity of product is also very high；Extraction is most common technique, but extraction process is complicated, and organic solvent consumption is big, extraction
The investment of equipment and operation cost are higher, and the processing of Discarded organic solvent is also a problem.
Summary of the invention
It, can be by zinc and chromium from sludge the invention proposes the method and apparatus of zinc and chromium in a kind of recycling heavy metal sewage sludge
In separate and realize purifying.
A kind of method of zinc and chromium in recycling heavy metal sewage sludge, it is comprised the steps of:
(1) it pre-processes: blocky heavy metal sewage sludge successively being crushed, is ground, obtain powder；
(2) it leaches: solid waste powder and leaching agent, regulator is subjected to mixing leaching；It is stood after leaching reaction, to solid
After liquid separation, supernatant remains to neutralize, and sinks mud after being filtered, washed, as Ordinary solid waste processing；
(3) it neutralizes: neutralizer is added in the leaching liquid obtained to step (2) and carries out acid-base neutralization；Neutralizer is after filtering
Remain evaporative crystallization；Filter residue remains to dissolve；
(4) it evaporates and is electrolysed: the filtrate obtained in step (3) being evaporated crystallization, obtains chromate；By step (3)
The filter residue acid adding of middle acquisition dissolves, and lysate carries out electrolysis processing, electrolytic zinc is obtained on cathode plate.
Wherein it is preferred to the pretreatment of the solid waste, the partial size of the solid powder of polished acquisition is 0.5-
2mm。
Wherein it is preferred to the leaching in the step (1), control mixeding liquid temperature is 40-90 DEG C；Leaching time is 20-
120min。
Wherein it is preferred to which the leaching agent is to contain any one in hydrogen peroxide, chlorine dioxide, sodium hypochlorite or several
The aqueous solution of kind；Regulator is sodium hydroxide.
Wherein it is preferred to which the additional amount of the leaching agent to leach in terms of the solute in agent solution, contains for chromium in solid waste
Measure 1-5 times of (quality)；After regulator is added in the step (2), manipulation condition is control pH value > 12.
Wherein it is preferred to sink mud filtering using filters pressing in the step (2)；The mud cake obtained after heavy mud filters pressing is adopted
With the alkali liquid washing of 1-10%.
Wherein it is preferred to leaching in the step (2) is multilevel leaching, the process route of multilevel leaching is, will be pre-
It is separated by solid-liquid separation after the solid powder leaching obtained in treatment process, supernatant sends to neutralization；Lower layer's sludge wouldn't be discharged；It uses at this time
The leaching liquid newly configured carries out second to lower layer's sludge and leaches, and stands after leaching, and supernatant pumps out storage, uses
In the first time leaching of next group charging；Leaching agent and regulator are added into the filtrate of filters pressing acquisition and mud cake cleaning solution, is matched
New leaching liquid is set, second of leaching for next group charging；Repeatedly.
Wherein it is preferred to the supernatant that obtains after leaching in the step (3), needs in and before to filter, use
It is sulfuric acid or hydrochloric acid with agent, the control terminal of neutralization reaction is pH value 7.0-8.2, and the filter method of neutralizer is filters pressing；It neutralizes
Liquid enters before vapo(u)rization system after filters pressing separates, and needs to carry out secondary filter, and filtering accuracy is 5-25 μm.
Wherein it is preferred to which the electrolysis in the step (4) is handled, cathode plate material is aluminium sheet or stainless steel plate；Anode plate
For graphite plate or lead alloy plate.
The device of zinc and chromium in a kind of recycling heavy metal sewage sludge, it is characterised in that: including multilevel leaching system, acid-base neutralization
System, evaporation and crystallization system, electrolysis system and medicine system；
The multilevel leaching system includes pulper, No. 1 leaching flow container, No. 2 leaching flow containers, No. 3 leaching flow containers and No. 1 pressure
Filter, No. 1 leaching flow container and No. 2 leaching flow containers are bi-directionally connected with pulper respectively, and the outlet of pulper and third leaching can connect
It connects, the slurry outlet of pulper is connect with No. 1 filter press, and No. 1 filter press filtrate outlet is connect with the import of No. 2 leaching cans；
The acid-base neutralization system, including No. 1 filter, neutralizing tank, No. 2 filter presses and filtrate tanks are sequentially connected, No. 1
Filter is connect with third leaching can；
The evaporation and crystallization system includes No. 2 filters and evaporation and crystallization system, and feed liquor filter is connect with filtrate tanks；
The electrolysis system includes dissolving tank and electrolytic cell, and dissolving tank and No. 2 filter presses connect；
The medicine system includes acid storage tank, alkali storage tank and leaching agent storage tank, acid storage tank respectively with neutralizing tank and dissolving tank
Connection, alkali storage tank and leaching agent storage tank are connect with No. 2 leaching flow containers respectively.
Beneficial effects of the present invention:
1. zinc and chromium in heavy metal sewage sludge can be successfully separated using the technique and device that propose in the present invention, realize
The rate of recovery of waste resource recovery, zinc and chromium is respectively greater than 95% and 90%；The product income of acquisition is greater than operating cost, has real
Border application value；
2. remaining filter residue after leaching can be used as general waste processing, greatly reduce disposal costs；
3. leaching technology of the invention is multilevel leaching, the sealing and circulating of medicament is realized；
4. electrolysis process of the invention, the acid solution that electrolytic process generates is back to neutralization chamber utilization；By the above-mentioned means, most
The discharge for avoiding residual pharmacy of limits, reduces reagent cost.
Detailed description of the invention
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this
Some embodiments of invention are put after not making the creative labor for those of ordinary skill in the art, can be with
It obtains other drawings based on these drawings.
Fig. 1 is the flow diagram of zinc and chromium method in recycling heavy metal sewage sludge of the invention；
Fig. 2 is the schematic diagram of zinc and chromium device in recycling heavy metal sewage sludge proposed by the present invention.
In figure: 1. pulpers；No. 2.2 leaching flow containers；No. 3.3 leaching flow containers；No. 4.1 leaching flow containers；No. 5.1 filter presses；
No. 6.1 filters；7. neutralizing tank；No. 8.2 filter presses；9. filtrate tanks；10.2 number filter；11. evaporation and crystallization system；12.
Dissolving tank；13. electrolytic cell；14. acid storage tank；15. leaching agent storage tank；16. alkali storage tank
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, those of ordinary skill in the art put obtained every other after not making creative work
Embodiment shall fall within the protection scope of the present invention.
Embodiment 1
As shown in Fig. 2, the present embodiment provides the device of zinc and chromium in a kind of recycling heavy metal sewage sludge, including multilevel leaching system
System, acid-base neutralization system, evaporation and crystallization system, electrolysis system and medicine system；
Multilevel leaching system includes 2, No. 3 leaching flow containers of the leaching flow container of leaching flow container 4,2 of pulper 1,1 and No. 1 pressure
5, No. 1 leaching flow container 4 and No. 2 leaching flow container 2 of filter is bi-directionally connected with pulper 1 respectively, and the outlet of pulper 1 and third leach
Tank connection, the slurry outlet of pulper 1 are connect with No. 1 filter press 5, the import of No. 1 filter press 5 filtrate (liquid and No. 2 leaching cans
Connection；
Acid-base neutralization system, including it is sequentially connected No. 1 filter 6,7, No. 2 filter presses 8 of neutralizing tank and filtrate tanks 9,1
Filter 6 is connect with third leaching can；
Evaporation and crystallization system includes No. 2 filters 10 and evaporation and crystallization system 11, and feed liquor filter and filtrate tanks 9 connect
It connects；
Electrolysis system includes dissolving tank 12 and electrolytic cell 13, and dissolving tank and No. 2 filter presses connect；
Medicine system includes acid storage tank 14, alkali storage tank 16 and leaching agent storage tank 15, acid storage tank 14 respectively with neutralizing tank 7 and molten
It solves tank 12 to connect, alkali storage tank 16 and leaching agent storage tank 15 are connect with No. 2 leaching flow containers 2 respectively.
Wherein, the logical pump of material conveying between stream oriented device carries out.
Embodiment 2
The present embodiment provides the technical process of zinc and chromium in recycling heavy metal sewage sludge, are arranged using embodiment 1, work
Skill flow chart is as shown in Figure 1.
Heavy metal sewage sludge is the generation of Hubei electronic components fabrication factory containing chromium, waste containing zinc in the present embodiment, main
Ingredient is as follows:
Above-mentioned sludge is first fed into broken crusher machine, crusher discharging is pulverized into rod mill, polished to obtain
The partial size of the solid powder obtained is 0.5mm, and grinding machine discharging is delivered to pulper by screw(-type) feeder, by technical grade liquid alkaline
(30%), sodium hypochlorite (10%) and water are configured to leaching liquid in No. 2 leaching flow containers by a certain percentage, and the pH value of leaching liquid is
14.2, it is sent into pulper together, stirring leaches, and 40 DEG C of leaching temperature；Leaching time is 120min, and material dosage is 0.72 ton
Liquid alkaline/ton waste, 1.8 tons sodium/ton wastes, 0.5t water/ton waste；The mixed liquor that leaching finishes is stood in pulper
After 40min, supernatant is pumped into No. 3 leaching flow containers, in case later separation；Lower layer's sludge remains second of leaching, at this time at No. 2
Leaching liquid is configured according to the above ratio in leaching flow container, is pumped into pulper, stirring leaches, and 80 DEG C of leaching temperature；Leaching time is
20min, this is considered as secondary leaching, is heated to 40 DEG C, and leaching finishes after 20min, is then allowed to stand 40min, and supernatant is sent into No. 1 leaching
Liquid bath is taken, the first time leaching for next group charging.Heavy dredge pump enters filter press filters pressing, and pressing filtering liquid is discharged into No. 2 leaching slots, mud cake
It is washed with lye (5%), cleaning solution consumption is 0.5 ton/ton waste, is washed after alkali cleaning；Cleaning solution is discharged into No. 2 leachings together
Take liquid bath.By the mud cake after washing according to HJ/T299-2007 " solid waste-Leaching leaching method-sulfonitric method " group
Leaching experiment is knitted, detection is found, the concentration of the heavy metals such as copper, zinc, nickel, chromium, cadmium, lead in leachate is lower than GB5085.3-
Limit value specified in 2007 " hazardous waste judging standards-leaching characteristic identification "；Therefore it will be transported to a brickmaking factory outside this mud cake, it uses
In brickmaking.
Liquid alkaline and time sodium are added in No. 2 leaching liquid baths, additional amount is 0.6 ton of liquid alkaline/ton waste, 1.4 tons sodium/tons are useless
Object configures new leaching liquid, second of leaching for next group charging.After first batch materials leach, by No. 3 leaching cans
In separating liquid be sent into neutralizing tank, add sulfuric acid (98%) to be neutralized, neutralization reaction control terminal be pH=8.1；After neutralizing
Mixed liquor be sent into filter press filters pressing, filtrate is pumped into sodium chromate tank；After mud cake washing, flushing water is sent into sodium chromate tank together；Mud
Cake is sent into zinc sulfate dissolving tank, acid adding dissolution.The filtrate of sodium chromate tank is through more medium filter (filtering accuracy is 5 μm) filtering
Afterwards, two effect vapo(u)rization systems are sent into, evaporative crystallization obtains sodium chromate；Electrolytic cell (graphite sheet anode+aluminium is sent into after zinc sulfate dissolution
Plate cathode) electrolysis, electrolytic zinc is obtained on cathode plate.The rate of recovery of chromium and zinc is respectively 94.4% and 90.5%.
In the present embodiment, the liquor natrii hypochloritis that leaching agent is 10%, can also be water-soluble for hydrogen peroxide or chlorine dioxide
Liquid, the liquid alkaline in the present embodiment are sodium hydrate aqueous solution.
Wherein, electrolytic cell can also be stainless steel plate cathode and lead alloy plate anode.
Embodiment 3
The present embodiment provides the technical process of zinc and chromium in recycling heavy metal sewage sludge, are arranged using embodiment 1, work
Skill flow chart is as shown in Figure 1.
Heavy metal sewage sludge is the waste containing chromium that Hubei Leather Factory generates in the present embodiment, and main component is as follows:
Because Zn content is less in sludge, therefore only recycle chromium.
Sludge is after hammering broken, rod milling into shape, and obtaining partial size is 2mm powder, and powder is by manually sending to pulper, by technical grade liquid alkaline
(30%), secondary sodium (10%) and water are configured to leaching liquid in No. 2 leaching flow containers, and pH value 15 is sent into pulper together, stirring
Leaching, 90 DEG C of leaching temperature；Leaching time is 20min, and material dosage is 0.15 ton of liquid alkaline/ton waste, 3.9 tons sodium/tons
Waste, 0.5t water/ton waste；After the mixed liquor that leaching finishes is stood 30min in pulper, supernatant is pumped into No. 3 leachings
Flow container is taken, in case later separation；Lower layer's sludge remains second of leaching, configures according to the above ratio in No. 2 leaching flow containers at this time
Leaching liquid is pumped into pulper, and stirring leaches, and 80 DEG C of leaching temperature；Leaching time is 20min, this is considered as secondary leaching, has been leached
30min is stood after finishing, supernatant is sent into No. 1 leaching liquid bath, the first time leaching for next group charging.Heavy dredge pump enters filter press
Filters pressing, pressing filtering liquid are discharged into No. 2 leaching slots, mud cake washing；Cleaning solution is discharged into No. 2 leaching liquid baths together.Mud cake after washing is pressed
According to HJ/T299-2007 " solid waste-Leaching leaching method-sulfonitric method " tissue leaching experiment, detection discovery, leaching
The concentration of the heavy metals such as the copper in liquid, zinc, nickel, chromium, cadmium, lead is lower than GB5085.3-2007 " hazardous waste judging standard-leaching out
Out toxicity identify " specified in limit value；Therefore by this mud cake directly as the processing of general waste reclamation.
Liquid alkaline and time sodium are added in No. 2 leaching liquid baths, additional amount is 0.15 ton of liquid alkaline/ton waste, 1.2 tons sodium/tons
Waste configures new leaching liquid, second of leaching for next group charging.After first batch materials leach, No. 3 are leached
Separating liquid in tank is sent into neutralizing tank, and sulfuric acid (98%) is added to be neutralized, and it is pH=7.0 that neutralization reaction, which controls terminal,；It will neutralize
Mixed liquor afterwards is sent into bag filter filtering, and filtrate is pumped into sodium chromate tank；After mud cake washing, flushing water is sent into sodium chromate together
Tank；After mud cake is by the detection of method described in HJ/T299-2007, as the processing of general waste reclamation.The filtrate of sodium chromate tank is through more
After medium filter (filtering accuracy is 25 μm) filtering, two effect vapo(u)rization systems are sent into, evaporative crystallization obtains sodium chromate, waste liqouor
Rate is 92%.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (1)
1. the device of zinc and chromium in a kind of recycling heavy metal sewage sludge, it is characterised in that: including multilevel leaching system, acid-base neutralization system
System, evaporation and crystallization system, electrolysis system and medicine system；
The multilevel leaching system includes pulper, No. 1 leaching flow container, No. 2 leaching flow containers, No. 3 leaching flow containers and No. 1 filters pressing
Machine, No. 1 leaching flow container and No. 2 leaching flow containers are bi-directionally connected with pulper respectively, and the outlet of pulper connects with No. 3 leaching flow containers
It connects, the slurry outlet of pulper is connect with No. 1 filter press, and the import that No. 1 filter press filtrate outlet leaches flow container with No. 2 is connect；
The acid-base neutralization system, including No. 1 filter, neutralizing tank, No. 2 filter presses and filtrate tanks are sequentially connected, No. 1 filtering
Device is connect with No. 3 leaching flow containers；
The evaporation and crystallization system includes No. 2 filters and evaporation and crystallization system, and No. 2 filters are connect with filtrate tanks；
The electrolysis system includes dissolving tank and electrolytic cell, and dissolving tank and No. 2 filter presses connect；The cathode plate of the electrolytic cell
Material is aluminium sheet or stainless steel plate, and anode plate is graphite plate or lead alloy plate；
The medicine system includes that acid storage tank, alkali storage tank and leaching agent storage tank, acid storage tank are connect with neutralizing tank and dissolving tank respectively,
Alkali storage tank and leaching agent storage tank are connect with No. 2 leaching flow containers respectively.
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| CN109763141B (en) * | 2019-01-31 | 2021-02-05 | 白银原点科技有限公司 | Multi-metal leaching and recycling process |
| CN110804745A (en) * | 2019-11-28 | 2020-02-18 | 衡阳旭光锌锗科技有限公司 | Electrolytic zinc-zinc mud rinsing device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101066827A (en) * | 2007-06-05 | 2007-11-07 | 台州盛世环境工程有限公司 | Electroplating sludge treating and utilizing process |
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| CN101244860A (en) * | 2008-03-28 | 2008-08-20 | 北京清大国华环保科技有限公司 | Extremely-high concentration multi-species heavy metal waste liquid treatment method and apparatus |
| CN101570372B (en) * | 2009-05-05 | 2011-06-08 | 中国科学院长春应用化学研究所 | Method for purifying electroplating wastewater and comprehensively utilizing resources |
| CN101638719A (en) * | 2009-09-08 | 2010-02-03 | 北京矿冶研究总院 | Method for producing synthetic rutile by wet process |
| CN102517449A (en) * | 2011-12-16 | 2012-06-27 | 山东方圆有色金属技术服务有限公司 | Comprehensive recycling technique of valuable elements in smelting soot |
| CN102560126A (en) * | 2012-02-27 | 2012-07-11 | 中南大学 | Method for extracting gold and/or silver from sulfuric acid slag |
| CN102634657A (en) * | 2012-05-04 | 2012-08-15 | 金川集团有限公司 | Chlorination leaching method of nickel unclassified stores |
| CN204417562U (en) * | 2014-12-31 | 2015-06-24 | 北京清大国华环保科技有限公司 | A kind of device reclaiming zinc and chromium in heavy metal sewage sludge |
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Address after: 100085 Beijing Haidian District Shangdi Third Street Jiahua Building C Building C404 Co-patentee after: Ningxia Ningdong Qingdaohua Environmental Resources Co.,Ltd. Patentee after: GO HIGHER ENVIRONMENT GROUP Co.,Ltd. Address before: 100085 Beijing Haidian District Shangdi Third Street Jiahua Building C Building C404 Co-patentee before: NINGXIA NINGDONG QINGDA GUOHUA KAIHONG ENVIRONMENTAL RESOURCES Co.,Ltd. Patentee before: GO HIGHER ENVIRONMENT GROUP Co.,Ltd. |