CN106698728A - Method for treating mercury-containing wastewater - Google Patents
Method for treating mercury-containing wastewater Download PDFInfo
- Publication number
- CN106698728A CN106698728A CN201510408514.5A CN201510408514A CN106698728A CN 106698728 A CN106698728 A CN 106698728A CN 201510408514 A CN201510408514 A CN 201510408514A CN 106698728 A CN106698728 A CN 106698728A
- Authority
- CN
- China
- Prior art keywords
- mercury
- outer tube
- waste water
- reactor
- sodium sulfide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Removal Of Specific Substances (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention provides a method for treating mercury-containing wastewater, and the method comprises the following steps: (1) the mercury-containing wastewater and a sodium sulfide water solution are sent into a micro reactor for reacting, the micro reactor includes a reactor and a mixer arranged on the top of the reactor, and the mixer comprises an inner tube and an outer tube; the mercury-containing wastewater enters the outer tube of the mixer from a wastewater inlet, the flow rate is 2.5-50 L / S, the sodium sulfide water solution enters the inner tube of the mixer from a sodium sulfide water solution inlet, the flow rate is 0.025-0.5L / S; then the mercury-containing wastewater and the sodium sulfide water solution enter the reactor via the nozzle of the mixer; and (2) a reacted solution in the micro reactor is sent into a membrane separation unit for separation, under the action of a suction pump, the wastewater passes through a separation membrane to enter the other side of the separation membrane to achieve filtering liquid discharge. The method accelerates mixing, mass transfer and chemical reaction propulsion of mercury removing chemicals in the mercury-containing wastewater, the mercury-containing wastewater in the whole system totally passes through the separation membrane to filter to achieve up-to-standard discharge, sludge slag is totally reused in catalyst manufacturers, and the method is currently the most advanced and most perfect treatment process.
Description
Technical field
The present invention relates to a kind of mercury-containing waste water treatment method.
Background technology
Mercury is a kind of argenteous liquid metals, and mercury and mercuric compounds are all noxious materials, can be passed through
Various approach are invaded in human or animal's body, and its toxicity is accumulation, and wherein inorganic mercury is mainly accumulated in
Internal organ, accumulate in brains, skin and other parts on a small quantity.During the poisoning manifestations of mercury are typically generally chronic
Poison, mercury mainly influences the nervous centralis of humans and animals.The mercurous water energy up to 0~0.02mg/L makes fish
Poisoning, can make aquatic insects be poisoned up to 0.03mg/L, and the water that people drinks mercurous 50mg/L can be poisoned
It is lethal.
Because mercury has some special physics, chemical properties, so being widely applied to chemical industry and stone
The industrial departments such as oily chemical industry, pharmacy, paper pulp, papermaking, electrical equipment, electronics, instrument, wherein chlorine
What the electrolysis in mercury cell technology of alkalization work use, PVC industries were used all belongs to containing mercury catalyst, low mercury catalyst
In the application of mercury and mercuric compounds.
Mercury and mercuric compounds enter environment in " three wastes " form, as one of important pollutant, wherein containing
Mercury waste water is mainly derived from " three wastes " discharges such as chlorine industry, plastics industry, fur processing and pharmacy and contains
Mercury organic bactericide is used.
Conventional treatment of mercury-containing wastewater have sulphide precipitation, Coagulation Method, active carbon adsorption,
Ion-exchange, reduction filtration method, microorganism concentration method and wool absorption method etc..
Boratex is a kind of nonmetallic reduction agent, and it mainly generates Elemental Mercury and inclined with mercury ion after reaction
Boric acid, releasing hydrogen.NaBH per kg4The Elemental Mercury for reclaiming 2kg can be reacted.
Every oxidation-reduction potential is less than Hg2+Metal simple-substance, such as Cu, Zn, Fe, Mn, Mg,
Al etc., can be with the Hg in waste water2+There is displacement reaction in ion, by taking iron as an example, iron filings are dressed up and is filled out
Material tower, will occur following reaction when iron filings bed of the mercury-containing waste water by packed tower：
Fe+Hg2+=Fe2++Hg↓
Replace the speed of reaction and the pH value of waste water, temperature, the purity of metal, metal simple-substance and waste water
The factor such as contact area it is relevant.But organic mercury can not be reduced directly with metal, displacement, generally use oxygen
Agent (such as chlorine) is first destroyed, and is converted into inorganic mercury, and metal replacement is then used again.
Sulphide precipitation is a kind of current adopted dynamical method for removing hydrargyrum extensively, if waste water
In have excessive S2-During ion, can be by adding ferrous sulfate (FeSO4) and excessive S2-Ion is given birth to
Into iron sulfide precipitates.
Add a part of Fe2+, can be with the OH in waste water-Ions binding generates Fe (OH)2Or after oxidation
Generation Fe (OH)3, HgS suspended particulates few and small to quantity play co-precipitation and flocking settling
Effect.Add FeSO4Afterwards, the preferential precipitation of HgS is not interfered with.Because the solubility of the FeS of generation
Product (Ksp=3.7x10-19) big hundreds of millions times of solubility product than HgS.In actual production, first adjusted with lime
Section pH=8~9, waste water is in alkalescence, then adds FeSO4.Using the vulcanized sodium precipitation method removal of mercury, in making waste water
Mercury quantity is down to 1~0.1mg/L, can take iron dust filtration, charcoal absorption, flocculating agent precipitation etc., makes
Mercury content is down to 0.05~below 0.01mg/L in waste water.
Domestic the most frequently used adsorbent is activated carbon at present, and Static Adsorption is first precipitated, adsorbed afterwards.
Ion-exchange, by several resins dress post composition purification of waste water series, such mercury-containing waste water passes through
After several exchange columns, mercury is can't check in water outlet.But there is a problem of desorption and regeneration after resin adsorption saturation,
And the resin scrapped is at present also without good processing means.
Coagulating sedimentation, using lime as flocculating agent, to feeding lime in mercury-containing waste water, generation
Ca(OH)2, Ca (OH)2There is cohesion suction-operated to mercury, in the presence of having ferric ion,
Effect is more preferable.Make flocculating agent with aluminum sulfate and process mercury-containing waste water, effect is also preferable.After through coagulative precipitation,
Effluent quality mercury content can drop to below 0.05mg/L.
Solvent extraction and other methods, at present, foreign countries have using the dimethylbenzene of tri-iso-octylamine one to mercurous
Waste water is extracted, and after extraction, the extractant after Extraction of Mercury is stripped using nonacid salt,
To reclaim mercury.Additionally, external reclaim mercury, electrolysis recovery mercury, the ferrite precipitation method using microorganism
The removal of mercury, the sulfide precipitation-flotation partition method removal of mercury, what the country was being studied has the conversion method removal of mercury, contains
Humic acid coal absorption method removal of mercury etc..
All there is certain technical problem in currently used mercury-containing waste water treatment method, such as reducing process,
Sulphide precipitation, coagulant sedimentation etc. be unable to reach water outlet it is mercurous≤finger of 0.001~0.002mg/L
Mark, the Ksp values according to HgS can be seen that after being reacted using vulcanization method, the remaining Hg of waste water2+
0.001~below 0.002mg/L is fully achieved, but the vulcanization method case for just having used at present is come
See mainly there are two the reason for water outlet does not reach 0.001~below 0.002mg/L：
(1) diffusion velocity of purifying of sodium sulfide agent is inadequate：
Hg in mercury-containing waste water2+Concentration is general all very low, such as with the suitable sodium sulfide solution of concentration with give up
Water reacts, and the total Water of processed waste water will increase a lot, many in order to avoid there is such case
The higher of na concn preparation will be vulcanized, be allowed to not influence the total Water of mercury-containing waste water, therefore vulcanized sodium essence
The concentration of preparation is generally Hg2+The hundreds times thousands of times of ion, the volume of purifying of sodium sulfide agent namely contains
One or number one thousandth of hundreds of points of mercury waste water, when a small amount of high concentration sodium sulfide solution is added to greatly
After in the mercury-containing waste water of amount, how to make vulcanized sodium rapid dispersion, be unlikely to local excessive etc. and just become
It is particularly significant.
(2) mercuric sulphide that reaction is formed fails to efficiently separate
It is right either using coagulant precipitation or charcoal absorption because vulcanization mercury particle is very tiny
It is all less than optimal in tiny vulcanization mercury particle.
Current each enterprise generally uses the vulcanization method removal of mercury, but is limited by waste water mercury concentration, reaction typically compared with
Hardly possible is controlled, and the vulcanization mercury particle for being formed is difficult to efficiently separate, and is ultimately resulted in mercury in producing water after processing and is contained
Amount reaches 0.005mg/L reluctantly.Standard higher has been formulated in treatment of the new environmental law to mercury-containing waste water,
It is required that producing water Hg≤0.002mg/L, it appears that be down to 0.002mg/L difference less by 0.005mg/L,
But because reaction is, in the ppb orders of magnitude, to have completely passed into the category of micro-reaction, reaction difficulty is more
Greatly.
And method conventional at present, it is difficult to reach the requirement of national regulation.
The content of the invention
It is an object of the invention to provide a kind of mercury-containing waste water treatment method, to overcome what prior art was present
Defect.
The method of the present invention comprises the following steps：
(1) by mercury-containing waste water and sodium sulfide solution that pH is 6~9, by sending into microscale reactor
Reacted；
In described mercury-containing waste water, the content of mercury is>0.002~0.05mg/L；
Described sodium sulfide solution concentration is 0.8~1.2g/L；
The consumption of sodium sulfide solution, is calculated as with vulcanized sodium and mercury：
Vulcanized sodium: mercury=2~10: 1, mol ratio；
Preferably, vulcanized sodium: mercury=3~5: 1, mol ratio；
Described microscale reactor include reactor and set at the top of it be made up of inner and outer tubes it is mixed
Clutch；
Mercury-containing waste water is entered the outer tube of blender by waterwater entrance, and flow velocity is 2.5~50L/ seconds, vulcanized sodium
The aqueous solution is entered the inner tube of blender by sodium sulfide solution entrance, and flow velocity is 0.025~0.5L/ seconds；
Then the shower nozzle atomisation of blended device, mutually collides by the huge specific surface area of droplet, passes
Matter and reaction, enter back into reactor；
(2) and then by reacted solution feeding film separation unit in microscale reactor separated,
In the presence of suction pump, waste water enters the opposite side of film by seperation film, obtains cleaner liquid discharge；
And HgS, FeS, Fe (OH)2、Fe(OH)3Deng solid particle, the side for being trapped within film is formed
Filter cake, it is achieved thereby that the separation of mercury-containing waste water；
Further, present invention additionally comprises following steps：
Part cleaner liquid is passed through film separation unit, the filter cake recoil that the side to being trapped within film is formed
Wash, collect the liquid-solid mixture after recoil, dewatering unit is delivered to by Pulp pump, after dehydration
Mud cake as the raw material of catalyst manufacturer, can collect the water of abjection, return to film separation unit and enter again
Row UF membrane；
Described film separation unit, can be using conventional membrane separation assemblies, such as Shanghai power arteries and veins environmental protection equipment
Co., Ltd's trade mark is the membrane separation assemblies of Lymax/IMF；
Described part cleaner liquid is the 5~10% of cleaner liquid discharge gross weight；
In the cleaner liquid of discharge, ferrous sulfate is added, be used to remove excessive vulcanized sodium.
Because Mercury in Wastewater content is very low, but discharging standards are not reached, continued with
Into the field of micro-reaction, if the removal of mercury chemical agent for adding is also suitable concentration, process
The amount of efflux wastewater can expand even double afterwards；It is unfavorable if adding removal of mercury chemical concentration higher
Mixing, diffusion and reaction in it in mercury-containing waste water is complete.
The present invention uses microscale reactor, accelerate mixing of the removal of mercury chemical agent in mercury-containing waste water,
Mass transfer and chemical reaction motive force.Using the method for the present invention, whole system mercury-containing waste water 100% passes through
Membrane filtration qualified discharge, the reuse of body refuse 100% to catalyst producer is current most advanced most perfect treatment
Technique.
Brief description of the drawings
Fig. 1 is flow chart of the invention.
Fig. 2 is the structural representation of microscale reactor.
Fig. 3 is nozzle structure schematic diagram.
Specific embodiment
Referring to Fig. 1, the method for the present invention comprises the following steps：
(1) by mercury-containing waste water and sodium sulfide solution that pH is 6~9, by sending into microscale reactor
100 are reacted；
(2) and then by reacted solution feeding film separation unit 200 in microscale reactor separated,
In the presence of suction pump 400, waste water enters the opposite side of film by seperation film, obtains cleaner liquid row
Put；
And HgS, FeS, Fe (OH)2、Fe(OH)3Deng solid particle, the side for being trapped within film is formed
Filter cake, it is achieved thereby that the separation of mercury-containing waste water；
Further, present invention additionally comprises following steps：
Part cleaner liquid is passed through film separation unit, the filter cake recoil that the side to being trapped within film is formed
Wash, collect the liquid-solid mixture after recoil, dewatering unit 200 is delivered to by Pulp pump, after dehydration
Mud cake can as the raw material of catalyst manufacturer, collect abjection water, return film separation unit again
Carry out UF membrane；
Referring to Fig. 2 and Fig. 3, described microscale reactor 100 includes reactor 2 and sets at the top of it
Blender 1；
Described blender 1 includes outer tube 101 and inner tube 102, and described outer tube 101 is enclosed within interior
Outside pipe 102, the bottom of described outer tube 101 is provided with shower nozzle 103, described outer tube 101 it is upper
Portion is provided with waterwater entrance 104, and the top of described inner tube 102 is sodium sulfide solution entrance 105；
The middle part of described shower nozzle 103 is provided with trunnion 106；
The ratio between the described cross-sectional area of outer tube 101 and described cross-sectional area of inner tube 102 are：
The cross-sectional area of outer tube 101: cross-sectional area=1 of inner tube 102: 0.001~0.01；
The cross-sectional area of outer tube 101: cross-sectional area=1 of trunnion 106: 0.001~0.005；
Term " cross-sectional area of outer tube 101 " is that valid circulation area, i.e. outer tube 101 are transversal
The face gross area-the cross-sectional area of inner tube 102；
Preferably, spacing L is provided between described inner tube 102 and the lower end of outer tube 101, it is described
Spacing L is 5~20mm；
The spray angle α of described shower nozzle 103 is 55~65 °, preferably 60 °；
Preferably, diameter of the diameter of the end of described shower nozzle 103 less than or equal to outer tube 101.
Embodiment 1
The mercury-containing waste water treatment produced in calcium carbide process PVC production technology, waste water is mixed by traditional vulcanization
Solidifying method treatment, the Hg in waste water is in 0.005~0.02mg/L.
Using the flow of Fig. 1, the reactor of Fig. 2 and the shower nozzle of Fig. 3：
Wherein：
The ratio between the cross-sectional area of outer tube 101 and described cross-sectional area of inner tube 102 are：Outer tube
101 cross-sectional areas: cross-sectional area=1 of inner tube 102: 0.05；
The cross-sectional area of outer tube 101: cross-sectional area=1 of trunnion 106: 0.0025；
Term " cross-sectional area of outer tube 101 " is that valid circulation area, i.e. outer tube 101 are transversal
The face gross area-the cross-sectional area of inner tube 102；
Spacing L between the lower end of inner tube 102 and outer tube 101 is 15mm；
The spray angle α of shower nozzle 103 is 60 °；
The diameter of the end of described shower nozzle 103 is equal to the diameter of outer tube 101；
Basic parameter：
In waste water, mercury content is 0.005~0.02mg/L；
Sodium sulfide solution concentration：1g/L；
In terms of vulcanized sodium and mercury：Vulcanized sodium: mercury=3: 1, mol ratio；
Mercury-containing waste water flow velocity is 5L/ seconds, and sodium sulfide solution flow velocity is 0.05L/ seconds；
Operating process is as follows：
(1) by mercury-containing waste water, NaOH is added, adjusts pH to 7；
(2) and then by mercury-containing waste water and sodium sulfide solution, reacted by sending into microscale reactor；
Mercury-containing waste water enters blender 1 by waterwater entrance 104, and sodium sulfide solution is by sodium sulfide solution
Entrance 105 enters blender 1, then through the described atomisation of shower nozzle 103, by the huge ratio of droplet
Surface area is mutually collided, mass transfer and reaction, enters back into reactor 2, excessive to add ferrous sulfate, is used to
Excessive vulcanized sodium is removed, then pH to 8.5, stirring reaction 20 minutes are adjusted with alkali；
(3) and then by reacted solution feeding film separation unit 3 in microscale reactor separated,
In the presence of suction pump 4, waste water enters the opposite side of film, the cleaner liquid row of acquisition by seperation film
Put, wherein, Hg≤0.001mg/L；
And solid particle, be trapped within film side formed filter cake, it is achieved thereby that mercury-containing waste water point
From；
Part cleaner liquid is passed through film separation unit 3, the filter cake recoil that the side to being trapped within film is formed
Wash, collect the liquid-solid mixture after recoil, dewatering unit is delivered to by Pulp pump, after dehydration
Mud cake as the raw material of catalyst manufacturer, can collect the water of abjection, return to film separation unit and enter again
Row UF membrane；
Described film separation unit 3, can be using conventional membrane separation assemblies, such as Shanghai power arteries and veins environmental protection equipment
Co., Ltd's trade mark is the membrane separation assemblies of Lymax/IMF；
Described part cleaner liquid is the 5% of cleaner liquid discharge gross weight；
Produce water such as can supplement water with reuse to production process as caustic soda salt refining salt dissolving；
The mercury mud that dehydration is obtained can return to mercury catalyst producer, used as the raw material of Catalyst Production.
Embodiment 2
The mercury-containing waste water treatment of certain water based paint factory production, Hg is about 0.03~0.05mg/L in waste water,
PH is 8.
Using the flow of Fig. 1, the reactor of Fig. 2 and the shower nozzle of Fig. 3：
Wherein：
The ratio between the cross-sectional area of outer tube 101 and described cross-sectional area of inner tube 102 are：Outer tube
101 cross-sectional areas: cross-sectional area=1 of inner tube 102: 0.05；
The cross-sectional area of outer tube 101: cross-sectional area=1 of trunnion 106: 0.0025；
Term " cross-sectional area of outer tube 101 " is that valid circulation area, i.e. outer tube 101 are transversal
The face gross area-the cross-sectional area of inner tube 102；
Spacing L between the lower end of inner tube 102 and outer tube 101 is 45mm；
The spray angle α of shower nozzle 103 is 60 °；
The diameter of the end of described shower nozzle 103 is equal to the diameter of outer tube 101；
Basic parameter：
In waste water, mercury content is 0.03mg/L, and pH is 8；
Sodium sulfide solution concentration：1g/L；
In terms of vulcanized sodium and mercury：Vulcanized sodium: mercury=4: 1, mol ratio；
Mercury-containing waste water flow velocity is 5L/ seconds, and sodium sulfide solution flow velocity is 0.05L/ seconds；
Operating process is as follows：
(1) and then by mercury-containing waste water and sodium sulfide solution, reacted by sending into microscale reactor；
Mercury-containing waste water enters blender 1 by waterwater entrance 104, and sodium sulfide solution is by sodium sulfide solution
Entrance 105 enters blender 1, then through the described atomisation of shower nozzle 103, by the huge ratio of droplet
Surface area is mutually collided, mass transfer and reaction, enters back into reactor 2, excessive to add ferrous sulfate, is used to
Excessive vulcanized sodium is removed, then pH to 8.5, stirring reaction 40 minutes are adjusted with alkali；
(2) and then by reacted solution feeding film separation unit 3 in microscale reactor separated,
In the presence of suction pump 4, waste water enters the opposite side of film, the cleaner liquid row of acquisition by seperation film
Put, wherein, Hg≤0.001mg/L；
And solid particle, be trapped within film side formed filter cake, it is achieved thereby that mercury-containing waste water point
From；
Part cleaner liquid is passed through film separation unit 3, the filter cake recoil that the side to being trapped within film is formed
Wash, collect the liquid-solid mixture after recoil, dewatering unit is delivered to by Pulp pump, after dehydration
Mud cake as the raw material of catalyst manufacturer, can collect the water of abjection, return to film separation unit and enter again
Row UF membrane；
Described film separation unit 3, can be using conventional membrane separation assemblies, such as Shanghai power arteries and veins environmental protection equipment
Co., Ltd's trade mark is the membrane separation assemblies of Lymax/IMF；
Described part cleaner liquid is the 5% of cleaner liquid discharge gross weight；
Producing water can be with the supplement water of reuse to recirculated water；
The mercury mud that dehydration is obtained can return to mercury catalyst producer, used as the raw material of Catalyst Production.
Claims (10)
1. mercury-containing waste water treatment method, it is characterised in that comprise the following steps：
(1) by mercury-containing waste water and sodium sulfide solution that pH is 6~9, by sending into microscale reactor
(100) reacted；
Described microscale reactor include reactor and set at the top of it be made up of inner and outer tubes it is mixed
Clutch；
Mercury-containing waste water is entered the outer tube of blender by waterwater entrance, and flow velocity is 2.5~50L/ seconds, vulcanized sodium
The aqueous solution is entered the inner tube of blender by sodium sulfide solution entrance, and flow velocity is 0.025~0.5L/ seconds；
Then the shower nozzle of blended device enters reactor；
(2) and then by reacted solution feeding film separation unit in microscale reactor separated,
In the presence of suction pump, waste water enters the opposite side of film by seperation film, obtains cleaner liquid discharge.
2. method according to claim 1, it is characterised in that also comprise the following steps：
Part cleaner liquid is passed through film separation unit, the filter cake recoil that the side to being trapped within film is formed
Wash, collect the liquid-solid mixture after recoil, dewatering unit is delivered to by Pulp pump, collect abjection
Water, return to film separation unit carries out UF membrane again.
3. method according to claim 2, it is characterised in that described part cleaner liquid is filter
The 5~10% of clear liquid discharging gross weight.
4. method according to claim 1, it is characterised in that in the cleaner liquid of discharge, plus
Enter ferrous sulfate, be used to remove excessive vulcanized sodium.
5. method according to claim 1, it is characterised in that in described mercury-containing waste water, mercury
Content be>0.002~0.05mg/L；Described sodium sulfide solution concentration is 0.8~1.2g/L；
The consumption of sodium sulfide solution, is calculated as with vulcanized sodium and mercury：Vulcanized sodium: mercury=2~10: 1, rub
You compare.
6. method according to claim 5, it is characterised in that vulcanized sodium: mercury=3~5: 1, rub
You compare.
7. the method according to any one of claim 1~6, it is characterised in that described is micro anti-
Device (100) is answered including reactor 2 and the blender (1) at the top of it is set；
Described blender (1) includes outer tube (101) and inner tube (102), described outer tube
(101) it is enclosed within inner tube (102) outward, the bottom of described outer tube (101) is provided with shower nozzle (103),
The top of described outer tube (101) is provided with waterwater entrance (104), described inner tube (102)
Top is sodium sulfide solution entrance (105)；
Trunnion (106) is provided with the middle part of described shower nozzle (103).
8. method according to claim 7, it is characterised in that described outer tube (101) is horizontal
The ratio between area of section and described inner tube (102) cross-sectional area are：Outer tube (101) cross section
Area: inner tube (102) cross-sectional area=1: 0.001~0.01, outer tube (101) cross-sectional area:
Trunnion (106) cross-sectional area=1: 0.001~0.005.
9. method according to claim 8, it is characterised in that described inner tube and outer tube
It is 5~20mm that spacing L, described spacing L are provided between lower end；The jet angle of described shower nozzle 103
Degree α is 55~65 °.
10. method according to claim 8, it is characterised in that the end of described shower nozzle it is straight
Diameter of the footpath less than or equal to outer tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510408514.5A CN106698728A (en) | 2015-07-13 | 2015-07-13 | Method for treating mercury-containing wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510408514.5A CN106698728A (en) | 2015-07-13 | 2015-07-13 | Method for treating mercury-containing wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106698728A true CN106698728A (en) | 2017-05-24 |
Family
ID=58898419
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510408514.5A Pending CN106698728A (en) | 2015-07-13 | 2015-07-13 | Method for treating mercury-containing wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106698728A (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3711818B2 (en) * | 1999-11-05 | 2005-11-02 | 株式会社大林組 | Purification method for contaminated ground |
| CN101525188A (en) * | 2008-06-20 | 2009-09-09 | 阎绍才 | Treatment method of chemo-setting and membrane separation of waste water containing Hg |
| CN101880097A (en) * | 2010-01-18 | 2010-11-10 | 王鹤立 | Method and device for moving and quickly treating heavy metal-containing polluted water |
| CN102010086A (en) * | 2010-12-01 | 2011-04-13 | 新疆天业（集团）有限公司 | Method for treating mercury-containing wastewater with three-section continuous process |
| CN102145930A (en) * | 2011-02-21 | 2011-08-10 | 李开明 | Treatment method of mercury-containing wastewater |
| JP4794070B2 (en) * | 2001-06-26 | 2011-10-12 | 小名浜製錬株式会社 | Method for removing mercury contained in exhaust gas |
| CN102491477A (en) * | 2011-11-25 | 2012-06-13 | 中南大学 | Method and device for removing mercury from high concentration acid |
-
2015
- 2015-07-13 CN CN201510408514.5A patent/CN106698728A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3711818B2 (en) * | 1999-11-05 | 2005-11-02 | 株式会社大林組 | Purification method for contaminated ground |
| JP4794070B2 (en) * | 2001-06-26 | 2011-10-12 | 小名浜製錬株式会社 | Method for removing mercury contained in exhaust gas |
| CN101525188A (en) * | 2008-06-20 | 2009-09-09 | 阎绍才 | Treatment method of chemo-setting and membrane separation of waste water containing Hg |
| CN101880097A (en) * | 2010-01-18 | 2010-11-10 | 王鹤立 | Method and device for moving and quickly treating heavy metal-containing polluted water |
| CN102010086A (en) * | 2010-12-01 | 2011-04-13 | 新疆天业（集团）有限公司 | Method for treating mercury-containing wastewater with three-section continuous process |
| CN102145930A (en) * | 2011-02-21 | 2011-08-10 | 李开明 | Treatment method of mercury-containing wastewater |
| CN102491477A (en) * | 2011-11-25 | 2012-06-13 | 中南大学 | Method and device for removing mercury from high concentration acid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105884100B (en) | A kind of processing method of heavy metal wastewater thereby | |
| CN108002580B (en) | Method for treating acidic flue gas washing wastewater and application thereof | |
| CN106882884B (en) | A kind of method of chloride ion in recycling waste water | |
| CN110282767B (en) | Advanced treatment method and system for solid-oil-containing low-concentration heavy metal wastewater | |
| CN104445095A (en) | Method for purifying smelting waste acid | |
| CN102190345A (en) | Method for enriching low-concentration heavy metal in water by recyclable magnesium hydroxide adsorbent | |
| CN102936070A (en) | Method for treating mercury-containing wastewater during PVC (Polyvinyle Chloride) production through two-step process | |
| CN103553249A (en) | Method for acid separation and heavy metal recovery in electroplating waste liquor | |
| Yu et al. | Research progress on the removal, recovery and direct high-value materialization of valuable metal elements in electroplating/electroless plating waste solution | |
| CN103011347B (en) | Method for carrying out electrolytic treatment on copper-containing electroplating wastewater and recycling copper | |
| CN102627366B (en) | Method for treating vanadium pentoxide wastewater and circularly utilizing resources | |
| CN106315947A (en) | Processing system and processing technology for industrial sewage containing heavy metal | |
| CN107698092A (en) | A kind of packaged type fluorine-containing wastewater treatment method and device | |
| CN105036453A (en) | Organic wastewater treatment and recycling method | |
| CN102442748B (en) | Deep treatment method of naphthenic acid wastewater | |
| CN110038647A (en) | A kind of method of electrolysed saline solution highly efficient regeneration resin | |
| CN105502765A (en) | System and method for treating desulfurization wastewater and recycling resources cooperatively | |
| CN112125436A (en) | Wastewater treatment method for recovering copper and nickel from electroplating comprehensive wastewater | |
| CN103043834A (en) | Rear earth smelting wastewater treatment process | |
| CN102020382B (en) | Treatment method of industrial waste water containing diazodinitrophenol | |
| CN100348519C (en) | Process for treating coking waste water containing phenol and cyanogen by physical chemistry method and special device therefor | |
| CN207567053U (en) | A kind of packaged type fluorine-containing waste water processing apparatus | |
| CN107473319B (en) | Method for recovering cationic heavy metals in water through phase change regulation | |
| CN107381705A (en) | A kind of method of a variety of cation heavy metals in phase transformation regulation and control separation and recovery water | |
| CN106698728A (en) | Method for treating mercury-containing wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20170524 |
|
| WD01 | Invention patent application deemed withdrawn after publication |