CN105753235A - 3, 3', 4, 4'-tetraaminobiphenyl wastewater comprehensive treatment and resource utilization method - Google Patents
3, 3', 4, 4'-tetraaminobiphenyl wastewater comprehensive treatment and resource utilization method Download PDFInfo
- Publication number
- CN105753235A CN105753235A CN201610125698.9A CN201610125698A CN105753235A CN 105753235 A CN105753235 A CN 105753235A CN 201610125698 A CN201610125698 A CN 201610125698A CN 105753235 A CN105753235 A CN 105753235A
- Authority
- CN
- China
- Prior art keywords
- tetra
- amino
- biphenyl
- ion exchange
- resource utilization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/16—Halides of ammonium
- C01C1/164—Ammonium chloride
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G3/00—Compounds of copper
- C01G3/04—Halides
- C01G3/05—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treatment Of Water By Ion Exchange (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention relates to a 3, 3', 4, 4'-tetraaminobiphenyl wastewater comprehensive treatment and resource utilization method. The method includes the following steps in order: employing an ion exchange system to recover low concentration copper ions from the 3, 3', 4, 4'-tetraaminobiphenyl wastewater, with the filling resin of the ion exchange system being macroporous chelating resin; adjusting the pH value of the treated wastewater to 7-7.5, then carrying out evaporation concentration crystallization by a crystallizing evaporator to obtain an ammonium chloride product, crystallization filtrate and distilled water, reusing the crystallization filtrate for the synthesis reaction of the 3, 3', 4, 4'-tetraaminobiphenyl product, and subjecting the distilled water to up-to-standard discharge. The method not only solves the environmental pollution problem of heavy metal copper ions and ammonia-nitrogen wastewater, but also improves the recovery and utilization rate of resources in production wastewater, and is environmentally friendly, thus having good application prospects.
Description
Technical field
The present invention relates to a kind of wastewater comprehensive treatment and resource utilization method, particularly one 3,3 ', 4,4 '-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method.
Background technology
3,3 ', 4,4 '-tetra-amino-biphenyl (English abbreviation DAB), structure shown in formula I, is a kind of important fine-chemical intermediate, is mainly used in synthesizing heat-resisting macromolecule resin and synthetic fibers, the huge market demand.
Chinese patent CN201510663536.6 discloses a kind of 3,3 ', 4, the continuous preparation method of 4 '-tetra-amino-biphenyl, by melted 3,3 '-dichloro-benzidine squeezes into reactor through high-pressure pump, again ammoniacal liquor and cupric chloride mixtures are squeezed into reactor, at 0.4MPa, carry out aminating reaction at 140 DEG C, after reaction completely, send into retracting device after pressure-reducing valve decompression discharging, distill out excess ammonia, separate and remove insoluble matter, filtration is refining to obtain 3,3 ', 4,4 '-tetra-amino-biphenyl, filtered fluid contains Cu2+150～200mg/L, ammonia nitrogen 800～1000mg/L, COD cr substantially 2000mg/L, in prior art to the method for comprehensive utilization of filtered fluid as described in CN200810139137.X.
The reaction equation of aminating reaction is as follows:
CN200810139137.X discloses by a kind of waste ammonia mother liquid from 4-aminobiphenyl product production method of comprehensive utilization, by tetra-amino-biphenyl deposed ammonia, is passed through sulfuric acid and neutralizes, and then evaporative crystallization separates.The method obtains ammonium sulfate product and contains heavy metal copper ion, and copper ion does not recycle, and circulating and evaporating energy consumption is big, and the wasting of resources is big.
Summary of the invention
It is an object of the invention to overcome the most methodical shortcoming, it is provided that a kind of 3,3 ', 4,4 '-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method so that copper ion and ammonia nitrogen in waste liquid obtain Appropriate application.
For solving above technical problem, the present invention adopts the following technical scheme that
A kind of 3,3 ', 4,4 '-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, described 3,3 ', 4, Cu in 4 '-tetra-amino-biphenyl waste water2+Content is 150～200mg/L, and ammonia-nitrogen content is 800～1000mg/L, and COD cr is 1900～2100mg/L；
The described comprehensive regulation and resource utilization method include the following steps carried out successively:
(1), metal copper ion is removed: to described 3,3 ', 4,4 '-tetra-amino-biphenyl waste water, use ion exchange system to reclaim the copper ion of low concentration, the resin that described ion exchange system is filled is macroporous chelate resin；
(2), evaporating, concentrating and crystallizing: the pH value adjusting the waste water after step (1) processes is 7～7.5, the most crystallized evaporator evaporation condensing crystallizing, obtain ammonium chloride product salt, crystallization filtrate and distilled water, described crystallization filtrate recycle is in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production, described distilled water qualified discharge.
Preferably, described macroporous chelate resin is the D401 macropore polystyrene chelating ion exchange resin purchased from upper starfish resinification work Co., Ltd.
Preferably, in step (1), described 3,3 ', 4,4 '-tetra-amino-biphenyl waste water is 3～5min in the time of staying of ion exchange column.
Preferably, in step (1), described 3,3 ', 4, the intake of 4 '-tetra-amino-biphenyl waste water is 1200～1500L/m with the volume ratio of the ion exchange column of described ion exchange system3。
Preferably, when resolving ion exchange column, selecting mass percentage concentration is the resolving hydrochloric acid resin of 10～30%, obtains copper chloride solution, copper chloride solution as catalytic agent reuse in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production.
It is further preferred that the concentration of described copper chloride solution is 10～15g/L.
Preferably, in step (2), use mass percentage concentration be 25～30% hydrochloric acid adjust the pH value of waste water after step (1) processes.
Preferably, in step (2), described crystallizing evaporator is MVR crystallizing evaporator.
Preferably, described 3,3 ', 4,4 '-tetra-amino-biphenyl waste water is 3,3 ', 4, after the synthetic reaction of 4 '-4-aminobiphenyl product production is complete, through distilling out excess ammonia, separate and remove insoluble matter, filter and be refining to obtain 3,3 ', 4, the filtered fluid after 4 '-4-aminobiphenyl product production.
Due to the utilization of technique scheme, the present invention compared with prior art has the advantage that
Owing to have employed the comprehensive regulation and the resource utilization method of the present invention, solve the pollution problem to environment of heavy metal copper ion and ammonia nitrogen waste water, improve simultaneously and produce resource recycling rate in waste water, and environmentally friendly, have a good application prospect.The present invention is by controlling pH so that reactant liquor is little to the injury of reactor, and saves the consumption of acid, thus has saved cost.Carry out the present invention and heavy metal copper ion can be converted to copper chloride solution, be then circulated utilization, both reduced environmental pollution, and reduced again production cost；The present invention can obtain ammonium chloride crystals filtrate, and this crystallization filtrate is circulated utilization, has both improve product yield, has reduced again waste water control difficulty；The ammonium chloride product salt quality that the present invention obtains is good, and purity is high, can carry out resource recycling.Further, the copper chloride that the present invention obtains and crystallization filtrate can be back to 3,3 ', 4, in the synthetic reaction of 4 '-tetra-amino-biphenyl and the carrying out of synthetic reaction and product quality will not be produced impact.
Detailed description of the invention
Below in conjunction with specific embodiment, the present invention is described in further details.Should be understood that these embodiments are for the general principle of the present invention, principal character and advantage are described, and the present invention is not limited by the following examples.The implementation condition used in embodiment can do adjustment further according to specific requirement, and not marked implementation condition is usually the condition in normal experiment.
Embodiment 1
(1), metal copper ion is removed:
1. 3,3 ', 4 are collected, 4 '-tetra-amino-biphenyl waste water 8000L (wherein, Cu2+Content is 150mg/L, ammonia-nitrogen content is 1000mg/L, COD cr is 2000mg/L), be added slowly to height 0.5 meter, volume is in the ion exchange column of 6 cubic metres, resin in ion exchange column is the D401 macropore polystyrene chelating ion exchange resin purchased from upper starfish resinification work Co., Ltd, waste liquid is 3 minutes in the time of staying of ion exchange column, and by collecting purified waste water after ion exchange column, Cu in waste water content is 1ppm after testing.
2. the hydrochloric acid of 10% is used to be slowly dropped in ion exchange column, hydrochloric acid is 2 minutes in the time of staying of ion exchange column, by obtaining the copper chloride solution of 100L 12g/L after ion exchange column, this copper chloride solution can be as catalytic agent reuse in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production.
(2), evaporating, concentrating and crystallizing
The waste liquid of above-mentioned removal copper ion is added the hydrochloric acid of 30%, allocates pH value of waste water 7；Squeeze into MVR crystallizing evaporator condensing crystallizing, separate to obtain the ammonium chloride product salt that 25kg, purity are 99.6%, 100L 40g/L ammonium chloride crystals filtrate (ammonium chloride crystals filtrate can direct reuse in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production) and 7500L distilled water (ammonia nitrogen 10mg/L, COD cr50mg/L in distilled water).
Embodiment 2
(1), metal copper ion is removed:
1. 3,3 ', 4 are collected, 4 '-tetra-amino-biphenyl waste water 8000L (wherein, Cu2+Content is 200mg/L, ammonia-nitrogen content is 800mg/L, COD cr is 2000mg/L), be added slowly to height 0.5 meter, volume is in the ion exchange column of 6 cubic metres, resin in ion exchange column is the D401 macropore polystyrene chelating ion exchange resin purchased from upper starfish resinification work Co., Ltd, waste liquid is 5 minutes in the time of staying of ion exchange column, and by collecting purified waste water after ion exchange column, Cu in waste water content is 1.1ppm after testing.
2. the hydrochloric acid of 30% is used to be slowly dropped in ion exchange column, hydrochloric acid is 2 minutes in the time of staying of ion exchange column, by obtaining the copper chloride solution of 94L 17g/L after ion exchange column, this copper chloride solution can be as catalytic agent reuse in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production.
(2), evaporating, concentrating and crystallizing
The waste liquid of above-mentioned removal copper ion is added the hydrochloric acid of 30%, allocates pH value of waste water 7.5；Squeeze into MVR crystallizing evaporator condensing crystallizing, separate to obtain the ammonium chloride product salt that 20kg, purity are 99.7%, 89L 41g/L ammonium chloride crystals filtrate (ammonium chloride crystals filtrate can direct reuse in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production) and 7600L distilled water (ammonia nitrogen 12mg/L, COD cr45mg/L in distilled water).
Embodiment 3
(1), metal copper ion is removed:
1. 3,3 ', 4 are collected, 4 '-tetra-amino-biphenyl waste water 8500L (wherein, Cu2+Content is 180mg/L, ammonia-nitrogen content is 900mg/L, COD cr is 2000mg/L), be added slowly to height 0.5 meter, volume is in the ion exchange column of 6 cubic metres, resin in ion exchange column is the D401 macropore polystyrene chelating ion exchange resin purchased from upper starfish resinification work Co., Ltd, waste liquid is 4 minutes in the time of staying of ion exchange column, and by collecting purified waste water after ion exchange column, Cu in waste water content is 1ppm after testing.
2. the hydrochloric acid of 20% is used to be slowly dropped in ion exchange column, hydrochloric acid is 2 minutes in the time of staying of ion exchange column, by obtaining the copper chloride solution of 90L 17g/L after ion exchange column, this copper chloride solution can be as catalytic agent reuse in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production.
(2), evaporating, concentrating and crystallizing
The waste liquid of above-mentioned removal copper ion is added the hydrochloric acid of 30%, allocates pH value of waste water 7.3；Squeeze into MVR crystallizing evaporator condensing crystallizing, separate to obtain the ammonium chloride product salt that 25.3kg, purity are 99.6%, 95L 40g/L ammonium chloride crystals filtrate (ammonium chloride crystals filtrate can direct reuse in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production) and 7800L distilled water (ammonia nitrogen 10mg/L, COD cr43mg/L in distilled water).
Comparative example 1
(1), metal copper ion is removed:
1. 3,3 ', 4 are collected, 4 '-tetra-amino-biphenyl waste water 8000L (wherein, Cu2+Content is 200mg/L, ammonia-nitrogen content is 800mg/L, COD cr is 2000mg/L), be added slowly to height 0.5 meter, volume is in the ion exchange column of 6 cubic metres, resin in ion exchange column be city available from aminodithioformic acid type chelating resin, waste liquid is 5 minutes in the time of staying of ion exchange column, and by collecting purified waste water after ion exchange column, Cu in waste water content is 80ppm after testing.
2. using the hydrochloric acid of 30% to be slowly dropped in ion exchange column, hydrochloric acid is 2 minutes in the time of staying of ion exchange column, by obtaining the copper chloride solution of 100L 15.1g/L after ion exchange column.
(2), evaporating, concentrating and crystallizing
The waste liquid of above-mentioned removal copper ion is added the hydrochloric acid of 30%, allocates pH value of waste water 7.5；Squeeze into MVR crystallizing evaporator condensing crystallizing, separate to obtain the ammonium chloride product salt that 19kg, purity are 99.2%, 90L 40g/L ammonium chloride crystals filtrate (ammonium chloride crystals filtrate can direct reuse in 3,3 ', 4, the synthetic reaction of 4 '-4-aminobiphenyl product production) and 7500L distilled water (ammonia nitrogen 12mg/L, COD cr50mg/L in distilled water).
Claims (9)
1. one kind 3,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterised in that: described 3, Cu in 3,4,4-tetra-amino-biphenyl waste water2+Content is 150 ~ 200mg/L, ammonia-nitrogen content be 800 ~ 1000mg/L, COD cr be 1900 ~ 2100mg/L；
The described comprehensive regulation and resource utilization method include the following steps carried out successively:
(1), metal copper ion is removed: to described 3,3,4,4-tetra-amino-biphenyl waste water, use ion exchange system to reclaim the copper ion of low concentration, the resin that described ion exchange system is filled is macroporous chelate resin；
(2), evaporating, concentrating and crystallizing: the pH value adjusting the waste water after step (1) processes is 7 ~ 7.5, the most crystallized evaporator evaporation condensing crystallizing, obtain ammonium chloride product salt, crystallization filtrate and distilled water, described crystallization filtrate recycle is in 3,3, the synthetic reaction of 4,4-4-aminobiphenyl product production, described distilled water qualified discharge.
The most according to claim 13,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterised in that: described macroporous chelate resin is the D401 macropore polystyrene chelating ion exchange resin purchased from upper starfish resinification work Co., Ltd.
The most according to claim 13,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterised in that: in step (1), described 3,3,4,4-tetra-amino-biphenyl waste water is 3 ~ 5min in the time of staying of ion exchange column.
The most according to claim 13,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterized in that: in step (1), described 3,3, the intake of 4,4-tetra-amino-biphenyl waste water is 1200 ~ 1500L/m with the volume ratio of the ion exchange column of described ion exchange system3。
The most according to any one of claim 1 to 43,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterised in that: when resolving ion exchange column, the resolving hydrochloric acid resin selecting mass percentage concentration to be 10 ~ 30%, obtain copper chloride solution, copper chloride solution as catalytic agent reuse in 3,3, the synthetic reaction of 4,4-4-aminobiphenyl product production.
The most according to claim 53,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterised in that: the concentration of described copper chloride solution is 10 ~ 15g/L.
The most according to claim 13,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterised in that: in step (2), the hydrochloric acid using mass percentage concentration to be 25 ~ 35% adjusts the pH value of the waste water after step (1) processes.
The most according to claim 13,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterised in that: in step (2), described crystallizing evaporator is MVR crystallizing evaporator.
The most according to claim 13,3,4,4-tetra-amino-biphenyl wastewater comprehensive treatment and resource utilization method, it is characterised in that: described 3,3,4,4-tetra-amino-biphenyl waste water is 3,3, after the synthetic reaction of 4,4-4-aminobiphenyl product production is complete, through distilling out excess ammonia, insoluble matter is removed in separation, filters and is refining to obtain 3,3, filtered fluid after 4,4-4-aminobiphenyl product production.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610125698.9A CN105753235A (en) | 2016-03-07 | 2016-03-07 | 3, 3', 4, 4'-tetraaminobiphenyl wastewater comprehensive treatment and resource utilization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610125698.9A CN105753235A (en) | 2016-03-07 | 2016-03-07 | 3, 3', 4, 4'-tetraaminobiphenyl wastewater comprehensive treatment and resource utilization method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105753235A true CN105753235A (en) | 2016-07-13 |
Family
ID=56332596
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610125698.9A Pending CN105753235A (en) | 2016-03-07 | 2016-03-07 | 3, 3', 4, 4'-tetraaminobiphenyl wastewater comprehensive treatment and resource utilization method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105753235A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4911213B1 (en) * | 1970-05-23 | 1974-03-15 | ||
| CN101643249A (en) * | 2008-08-08 | 2010-02-10 | 夏恩将 | Method for comprehensively using waste ammonia mother liquid from 4-aminobiphenyl product production |
| CN103086558A (en) * | 2013-02-18 | 2013-05-08 | 东江环保股份有限公司 | Treatment method of copper chloride hydroxide production wastewater |
| CN105111092A (en) * | 2015-10-15 | 2015-12-02 | 吴江梅堰三友染料化工有限公司 | Continuous preparation method of DAB (3,3'-diaminobenzidine) |
-
2016
- 2016-03-07 CN CN201610125698.9A patent/CN105753235A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4911213B1 (en) * | 1970-05-23 | 1974-03-15 | ||
| CN101643249A (en) * | 2008-08-08 | 2010-02-10 | 夏恩将 | Method for comprehensively using waste ammonia mother liquid from 4-aminobiphenyl product production |
| CN103086558A (en) * | 2013-02-18 | 2013-05-08 | 东江环保股份有限公司 | Treatment method of copper chloride hydroxide production wastewater |
| CN105111092A (en) * | 2015-10-15 | 2015-12-02 | 吴江梅堰三友染料化工有限公司 | Continuous preparation method of DAB (3,3'-diaminobenzidine) |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107459200B (en) | High-salt-content wastewater salinity resource recovery process | |
| CN108275819B (en) | Method for recycling ternary precursor washing wastewater | |
| CN104326612B (en) | A kind of method and system reclaiming salt from Waste Water Treatment | |
| CN110040748A (en) | Utilize the method for incineration of refuse flyash production sylvite and sodium salt | |
| CN104609633A (en) | Method and device for utilizing sewage containing ammonia and sodium | |
| CN103553138A (en) | Comprehensive utilization method for separating, concentrating and purifying manganese sulfate, magnesium sulfate and calcium sulfate in high-salt waste water | |
| CN105293584A (en) | Method for purifying manganese sulfate solution | |
| CN109912096A (en) | A kind of pretreated method of o-methyl formate benzene sulfonamide waste water sub-prime | |
| CN110981065A (en) | Treatment method of lithium battery industrial wastewater | |
| CN114314988A (en) | Iron phosphate wastewater treatment and salt recovery system and method | |
| CN111547892A (en) | Treatment method of ammonia nitrogen wastewater in manganese chemical industry | |
| CN102701476A (en) | Comprehensive utilization method of concentrated sea water or brackish water | |
| CN204310904U (en) | A kind of system reclaiming salt from Waste Water Treatment | |
| CN103265079A (en) | Method for recovering molybdenum from molybdenum containing waste acid of filament wire | |
| CN116425353A (en) | Ternary precursor wastewater treatment method | |
| CN110817907B (en) | Treatment system and method for purifying high-purity lithium carbonate | |
| CN1184077A (en) | Ion exchange process for producing potassium nitrate | |
| CN113860995B (en) | Recovery treatment process and treatment device for waste liquid produced in production of acetochlor | |
| CN106086405A (en) | A kind of purifying and impurity-removing method of high salt Chloride System | |
| CN103979727B (en) | The method of recycle-water and sulfate species from sulfuric acid rare earth factory effluent | |
| CN105753235A (en) | 3, 3', 4, 4'-tetraaminobiphenyl wastewater comprehensive treatment and resource utilization method | |
| JP2024509488A (en) | Systems and methods for direct lithium hydroxide production | |
| CN109422407B (en) | Method for treating catalyst production wastewater | |
| CN115676856A (en) | Method and system for extracting lithium from salt lake | |
| CN216273564U (en) | Ammonium nitrate wastewater treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20161019 Address after: 224631 Jiangsu province Yancheng City Xiangshui eco Chemical Industrial Park (Group Seven Wan Cun) Applicant after: Xiangshui Henryda Tech Chemical Co., Ltd. Address before: 215225 Jiangsu city of Suzhou province Wujiang City Pingwang town Mei Yan Shuangqiao Village Applicant before: Wujiang Meiyan Sanyou Dyestuff Chemical Co., Ltd. |
|
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160713 |