CN104944668A - Treatment method of ammonium chloride wastewater - Google Patents
Treatment method of ammonium chloride wastewater Download PDFInfo
- Publication number
- CN104944668A CN104944668A CN201510380439.6A CN201510380439A CN104944668A CN 104944668 A CN104944668 A CN 104944668A CN 201510380439 A CN201510380439 A CN 201510380439A CN 104944668 A CN104944668 A CN 104944668A
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- Prior art keywords
- water
- ammonium chloride
- ion
- waste
- effect
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- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 title claims abstract description 69
- 239000002351 wastewater Substances 0.000 title claims abstract description 69
- 238000000034 method Methods 0.000 title claims abstract description 51
- 235000019270 ammonium chloride Nutrition 0.000 title claims abstract description 35
- 238000001704 evaporation Methods 0.000 claims abstract description 30
- 230000008020 evaporation Effects 0.000 claims abstract description 30
- 239000012153 distilled water Substances 0.000 claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000005342 ion exchange Methods 0.000 claims abstract description 19
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims abstract description 13
- 239000011347 resin Substances 0.000 claims abstract description 11
- 229920005989 resin Polymers 0.000 claims abstract description 11
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 7
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 7
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 7
- 239000003513 alkali Substances 0.000 claims abstract description 6
- 239000010949 copper Substances 0.000 claims description 46
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 31
- 229910052802 copper Inorganic materials 0.000 claims description 31
- 239000007788 liquid Substances 0.000 claims description 30
- 150000002500 ions Chemical class 0.000 claims description 26
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 10
- CHRJZRDFSQHIFI-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;styrene Chemical compound C=CC1=CC=CC=C1.C=CC1=CC=CC=C1C=C CHRJZRDFSQHIFI-UHFFFAOYSA-N 0.000 claims description 5
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical group C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 5
- 150000003863 ammonium salts Chemical class 0.000 claims description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 5
- 229910052742 iron Inorganic materials 0.000 claims description 5
- -1 iron ion Chemical class 0.000 claims description 5
- RECVMTHOQWMYFX-UHFFFAOYSA-N oxygen(1+) dihydride Chemical compound [OH2+] RECVMTHOQWMYFX-UHFFFAOYSA-N 0.000 claims description 5
- 238000002203 pretreatment Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 239000010802 sludge Substances 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 5
- 239000012670 alkaline solution Substances 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 abstract description 2
- 229910001431 copper ion Inorganic materials 0.000 abstract 2
- 230000002378 acidificating effect Effects 0.000 abstract 1
- 239000013522 chelant Substances 0.000 abstract 1
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 238000004065 wastewater treatment Methods 0.000 abstract 1
- 239000002699 waste material Substances 0.000 description 4
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a treatment method of ammonium chloride wastewater, which comprises the following steps: pretreatment of ammonium chloride wastewater: regulating the pH value to 5.0-5.4; copper ion removal treatment: sending the pretreated wastewater into a 1# ion-exchange system to lower the copper ion content; ammonia nitrogen evaporation concentration treatment; and deep ammonium removal treatment: sending distilled water into a 2# ion-exchange system to perform deep ammonium removal treatment, adding an alkali solution into the distilled water to regulate the pH value to 6-8, thereby implementing discharge after reaching the standard. The ammonium chloride has higher stability and can not be easily decomposed and volatilized under acidic conditions, so that the ammonia nitrogen content in the distilled water is lower. Meanwhile, the 001*7 chelate resin has high ion-exchange adsorption capacity for ammonium, so that the ammonia nitrogen content achieves certain standard. The method effectively enhances the stability of the ammonium chloride wastewater treatment, reduces the ammonia nitrogen content to a lower value by using the ion-exchange resin, has the advantages of high stability and reliability and high treatment capacity, and is simple to operate.
Description
Technical field
The present invention relates to chemical field, particularly a kind for the treatment of process of ammonium chloride waste-water.
Background technology
The useful resources in tin waste liquid comprehensive utilization waste liquid is moved back in process, the waste water of some ammonium chlorides can be produced in process, ammonia-nitrogen content wherein in ammonium chloride waste-water is very high, if without process, very large harm is had to environment, do not meet the standard of directly discharge, out moving back ammonium chloride waste-water in tin waste liquid is at present generally first after ion-exchange copper removal ion processing, enter vapo(u)rization system, phlegma ammonia nitrogen≤100ppm, phlegma passes through biochemical treatment, make the standard that ammonia-nitrogen content reaches certain, but the treatment capacity of biochemical treatment is little, and the condition of each side all requires harsher when biochemical treatment, by the impact of biochemical processing process, after process, ammonia-nitrogen content is unstable.
Summary of the invention
The object of the present invention is to provide a kind for the treatment of capacity large and stablize, ammonia nitrogen amount can be down to lower, the treatment process of moving back ammonium chloride waste-water in tin waste liquid of discharging standards can be reached.
To achieve these goals, present invention employs following technical scheme:
A treatment process for ammonium chloride waste-water, comprises the steps:
The pre-treatment of S1, ammonium chloride waste-water
In ammonium chloride waste-water, add sheet alkali or concentration is the hydrochloric acid of 27 ~ 32%, make pH value in 5.0 ~ 5.4 scopes, reclaim the copper sludge in waste water through pressure filter solid-liquid separation, pretreated waste water carries out next step process;
S2, copper removal ion processing
Pretreated waste water is entered 1
#ion exchange system carries out copper removal ion processing, and cupric ion in copper removal ion waste water is down to 0.1 ~ 0.3ppm, and the pH of copper removal ion waste water is 1 ~ 2.5;
S3, the process of ammonia nitrogen evaporation concentration
Copper removal ion waste water is entered triple effect evaporation system and carry out the operation of ammonia nitrogen evaporation concentration, obtain distilled water and ammonium salt;
S4, the degree of depth are except the process of ammonium root
Distilled water is entered 2# ion exchange system and carry out the degree of depth except the process of ammonium root, the pH value of the distilled water after process is 2.0 ~ 3.0, Cu%=0.01 ~ 0.02ppm, N-NH
4 +=1 ~ 3ppm, COD=30 ~ 80ppm, adds alkaline solution in distilled water, and adjust ph to 6 ~ 8 realize qualified discharge.
Preferably, described alkaline solution to be concentration be 30% NaOH solution.
Further, pretreated Cu in waste water ion <1000ppm, iron ion <10ppm, pH value is 5.0 ~ 5.2.
Further, the parameter of triple effect evaporation system fortune is as follows: an effect vacuum tightness is-0.050 ~-0.040Mpa, and 1st effective evaporator temperature is 90 ~ 100 DEG C, and an effect separator liquid level is 1 ~ 1.2m; Two effect vacuum tightnesss are-0.080 ~-0.070Mpa, and 2nd effect evaporator temperature is 80 ~ 90 DEG C, and two effect separator liquid levels are 0.7 ~ 0.8m; Triple effect vacuum tightness is-0.095 ~-0.085Mpa, and triple effect evaporation actuator temperature is 60 ~ 70 DEG C, and triple effect separator liquid level is 0.9 ~ 1.1m.
Preferably, the parameter of triple effect evaporation system fortune is as follows: an effect vacuum tightness is-0.045Mpa, and 1st effective evaporator temperature is 95 DEG C, and an effect separator liquid level is 1.1m; Two effect vacuum tightnesss are-0.075Mpa, and 2nd effect evaporator temperature is 85 DEG C, and two effect separator liquid levels are 0.75m; Triple effect vacuum tightness is-0.090Mpa, and triple effect evaporation actuator temperature is 65 DEG C, and triple effect separator liquid level is 1.0 m.
Further, the performance perameter of the distilled water obtained in S3 is pH=3 ~ 4, Cu%=0.01 ~ 0.02ppm, N-NH
4 +≤ 100ppm.
Preferably, the resin that 1# ion exchange system is used is D403 macropore phenylethylene chelating ion exchange resin.
Preferably, 2# ion exchange system resin used is the resin of 001*7, i.e. with sulfonic Zeo-karb on vinylbenzene-divinylbenzene interpolymer.
The present invention in acid condition, ammonium chloride is more stable, not easily decompose, volatilize, make ammonia nitrogen in distilled water lower, simultaneously, 001*7 resin is strong to ammonium radical ion exchange adsorption ability, can guarantee that the ammonia nitrogen in waste water content after processing is at 1 ~ 3ppm, make the standard that ammonia-nitrogen content reaches certain, the present invention improves the stability of ammonium chloride waste-water process effectively, is down to lower by ion exchange resin by ammonia nitrogen amount, whole technique is not by the impact of other biochemical treatment conditions, reliable and stable, and simple to operate, treatment capacity is large.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of invention.
Embodiment
Now by reference to the accompanying drawings, the present invention is described in detail.
Embodiment one
With reference to accompanying drawing 1
A treatment process for ammonium chloride waste-water, comprises the steps:
The pre-treatment of S1, ammonium chloride waste-water
Sheet alkali is added or concentration is the hydrochloric acid of 30% in ammonium chloride waste-water, make pH value in 5.0 ~ 5.4 scopes, the copper sludge in waste water is reclaimed through pressure filter solid-liquid separation, pretreated Cu in waste water ion <1000ppm, iron ion <10ppm, pH value is 5.0 ~ 5.2, and pretreated waste water carries out next step process;
S2, copper removal ion processing
Pretreated waste water is entered and adopts 1 of D403 macropore phenylethylene chelating ion exchange resin
#ion exchange system carries out copper removal ion processing, and cupric ion in copper removal ion waste water is down to 0.1 ~ 0.3ppm, and the pH of copper removal ion waste water is 1 ~ 2.5;
S3, the process of ammonia nitrogen evaporation concentration
Copper removal ion waste water is entered triple effect evaporation system and carry out the operation of ammonia nitrogen evaporation concentration, obtain distilled water and ammonium salt, the parameter of triple effect evaporation system fortune is as follows: an effect vacuum tightness is-0.045Mpa, and 1st effective evaporator temperature is 95 DEG C, and an effect separator liquid level is 1.1m; Two effect vacuum tightnesss are-0.075Mpa, and 2nd effect evaporator temperature is 85 DEG C, and two effect separator liquid levels are 0.75m; Triple effect vacuum tightness is-0.090Mpa, and triple effect evaporation actuator temperature is 65 DEG C, and triple effect separator liquid level is 1.0 m; The performance perameter of distilled water is pH=3.6, Cu%=0.01ppm, N-NH
4 +≤ 100ppm.
S4, the degree of depth are except the process of ammonium root
Distilled water is entered the resin adopting 001*7, i.e. vinylbenzene-divinylbenzene interpolymer carries out the degree of depth except the process of ammonium root with the 2# ion exchange system of sulfonic Zeo-karb, the pH value of the distilled water after process is 2.5, Cu%=0.01ppm, N-NH
4 +=1ppm, COD=30ppm, add the NaOH solution of 30%, adjust ph to 7.2, realize qualified discharge in distilled water.
Embodiment 2
A treatment process for ammonium chloride waste-water, comprises the steps:
The pre-treatment of S1, ammonium chloride waste-water
Sheet alkali is added or concentration is the hydrochloric acid of 27% in ammonium chloride waste-water, make pH value in 5.0 ~ 5.4 scopes, the copper sludge in waste water is reclaimed through pressure filter solid-liquid separation, pretreated Cu in waste water ion <1000ppm, iron ion <10ppm, pH value is 5.0 ~ 5.2, and pretreated waste water carries out next step process;
S2, copper removal ion processing
Pretreated waste water is entered and adopts 1 of D403 macropore phenylethylene chelating ion exchange resin
#ion exchange system carries out copper removal ion processing, and cupric ion in copper removal ion waste water is down to 0.1 ~ 0.3ppm, and the pH of copper removal ion waste water is 1 ~ 2.5;
S3, the process of ammonia nitrogen evaporation concentration
Copper removal ion waste water is entered triple effect evaporation system and carry out the operation of ammonia nitrogen evaporation concentration, obtain distilled water and ammonium salt, the parameter of triple effect evaporation system fortune is as follows: an effect vacuum tightness is-0.050Mpa, and 1st effective evaporator temperature is 90 DEG C, and an effect separator liquid level is 1m; Two effect vacuum tightnesss are-0.080Mpa, and 2nd effect evaporator temperature is 80 DEG C, and two effect separator liquid levels are 0.7m; Triple effect vacuum tightness is-0.095Mpa, and triple effect evaporation actuator temperature is 60 DEG C, and triple effect separator liquid level is 0.9m, and the performance perameter of distilled water is pH=3, Cu%=0.01ppm, N-NH
4 +≤ 100ppm.
S4, the degree of depth are except the process of ammonium root
Distilled water is entered the resin adopting 001*7, i.e. vinylbenzene-divinylbenzene interpolymer carries out the degree of depth except the process of ammonium root with the 2# ion exchange system of sulfonic Zeo-karb, the pH value of the distilled water after process is 2.0 ~ 3.0, Cu%=0.02ppm, N-NH
4 +=3ppm, COD=80ppm, add the NaOH solution of 30%, adjust ph to 6 ~ 8, realize qualified discharge in distilled water.
Embodiment 3
A treatment process for ammonium chloride waste-water, comprises the steps:
The pre-treatment of S1, ammonium chloride waste-water
Sheet alkali is added or concentration is the hydrochloric acid of 32% in ammonium chloride waste-water, make pH value in 5.0 ~ 5.4 scopes, the copper sludge in waste water is reclaimed through pressure filter solid-liquid separation, pretreated Cu in waste water ion <1000ppm, iron ion <10ppm, pH value is 5.0 ~ 5.2, and pretreated waste water carries out next step process;
S2, copper removal ion processing
Pretreated waste water is entered and adopts 1 of D403 macropore phenylethylene chelating ion exchange resin
#ion exchange system carries out copper removal ion processing, and cupric ion in copper removal ion waste water is down to 0.1 ~ 0.3ppm, and the pH of copper removal ion waste water is 1 ~ 2.5;
S3, the process of ammonia nitrogen evaporation concentration
Copper removal ion waste water is entered triple effect evaporation system and carry out the operation of ammonia nitrogen evaporation concentration, obtain distilled water and ammonium salt, the parameter of triple effect evaporation system fortune is as follows: an effect vacuum tightness is-0.040Mpa, and 1st effective evaporator temperature is 100 DEG C, and an effect separator liquid level is 1.2m; Two effect vacuum tightnesss are-0.070Mpa, and 2nd effect evaporator temperature is 90 DEG C, and two effect separator liquid levels are 0.8m; Triple effect vacuum tightness is-0.085Mpa, and triple effect evaporation actuator temperature is 70 DEG C, and triple effect separator liquid level is 1.1m; The performance perameter of distilled water is pH=4, Cu%=0.02ppm, N-NH
4 +≤ 100ppm.
S4, the degree of depth are except the process of ammonium root
Distilled water is entered the resin adopting 001*7, i.e. vinylbenzene-divinylbenzene interpolymer carries out the degree of depth except the process of ammonium root with the 2# ion exchange system of sulfonic Zeo-karb, the pH value of the distilled water after process is 2.0 ~ 3.0, Cu%=0.05pm, N-NH
4 +=1.5ppm, COD=60ppm, add the NaOH solution of 30%, adjust ph to 6 ~ 8, realize qualified discharge in distilled water.
Above-described embodiment of the present invention, does not form limiting the scope of the present invention.Any amendment done within the spirit and principles in the present invention, equivalent replacement and improvement etc., all should be included within claims of the present invention.
Claims (8)
1. a treatment process for ammonium chloride waste-water, is characterized in that, comprises the steps:
The pre-treatment of S1, ammonium chloride waste-water
In ammonium chloride waste-water, add sheet alkali or concentration is the hydrochloric acid of 27 ~ 32%, make pH value in 5.0 ~ 5.4 scopes, reclaim the copper sludge in waste water through pressure filter solid-liquid separation, pretreated waste water carries out next step process;
S2, copper removal ion processing
Pretreated waste water is entered 1
#ion exchange system carries out copper removal ion processing, and cupric ion in copper removal ion waste water is down to 0.1 ~ 0.3ppm, and the pH of copper removal ion waste water is 1 ~ 2.5;
S3, the process of ammonia nitrogen evaporation concentration
Copper removal ion waste water is entered triple effect evaporation system and carry out the operation of ammonia nitrogen evaporation concentration, obtain distilled water and ammonium salt;
S4, the degree of depth are except the process of ammonium root
Distilled water is entered 2# ion exchange system and carry out the degree of depth except the process of ammonium root, the pH value of the distilled water after process is 2.0 ~ 3.0, Cu%=0.01 ~ 0.02ppm, N-NH
4 +=1 ~ 3ppm, COD=30 ~ 80ppm, adds alkaline solution in distilled water, and adjust ph to 6 ~ 8 realize qualified discharge.
2. the treatment process of a kind of ammonium chloride waste-water according to claim 1, is characterized in that, described alkaline solution to be concentration be 30% NaOH solution.
3. the treatment process of a kind of ammonium chloride waste-water according to claim 1, is characterized in that, pretreated Cu in waste water ion <1000ppm, iron ion <10ppm, pH value is 5.0 ~ 5.2.
4. the treatment process of a kind of ammonium chloride waste-water according to claim 1, it is characterized in that, the parameter of triple effect evaporation system fortune is as follows: an effect vacuum tightness is-0.050 ~-0.040Mpa, and 1st effective evaporator temperature is 90 ~ 100 DEG C, and an effect separator liquid level is 1 ~ 1.2m; Two effect vacuum tightnesss are-0.080 ~-0.070Mpa, and 2nd effect evaporator temperature is 80 ~ 90 DEG C, and two effect separator liquid levels are 0.7 ~ 0.8m; Triple effect vacuum tightness is-0.095 ~-0.085Mpa, and triple effect evaporation actuator temperature is 60 ~ 70 DEG C, and triple effect separator liquid level is 0.9 ~ 1.1m.
5. the treatment process of a kind of ammonium chloride waste-water according to claim 4, is characterized in that, the parameter of triple effect evaporation system fortune is as follows: an effect vacuum tightness is-0.045Mpa, and 1st effective evaporator temperature is 95 DEG C, and an effect separator liquid level is 1.1m; Two effect vacuum tightnesss are-0.075Mpa, and 2nd effect evaporator temperature is 85 DEG C, and two effect separator liquid levels are 0.75m; Triple effect vacuum tightness is-0.090Mpa, and triple effect evaporation actuator temperature is 65 DEG C, and triple effect separator liquid level is 1.0 m.
6. the treatment process of a kind of ammonium chloride waste-water according to claim 1, is characterized in that, the performance perameter of the distilled water obtained in S3 is pH=3 ~ 4, Cu%=0.01 ~ 0.02ppm, N-NH
4 +≤ 100ppm.
7. the treatment process of a kind of ammonium chloride waste-water according to claim 1, is characterized in that, 1# ion exchange system resin used is D403 macropore phenylethylene chelating ion exchange resin.
8. the treatment process of a kind of ammonium chloride waste-water according to claim 1, is characterized in that, 2# ion exchange system resin used is the resin of 001*7, i.e. with sulfonic Zeo-karb on vinylbenzene-divinylbenzene interpolymer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510380439.6A CN104944668B (en) | 2015-07-02 | 2015-07-02 | Treatment method of ammonium chloride wastewater |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510380439.6A CN104944668B (en) | 2015-07-02 | 2015-07-02 | Treatment method of ammonium chloride wastewater |
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| Publication Number | Publication Date |
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| CN104944668A true CN104944668A (en) | 2015-09-30 |
| CN104944668B CN104944668B (en) | 2017-04-12 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105601014A (en) * | 2015-12-28 | 2016-05-25 | 江苏瑞达环保科技有限公司 | Ammonia-nitrogen wastewater resourceful treatment system and treatment method of ammonia-nitrogen wastewater resourceful treatment system |
| CN107586958A (en) * | 2017-08-25 | 2018-01-16 | 金川集团股份有限公司 | A kind of method of ammonium root recycling in waste water of noble metal containing ammonium |
| CN108658374A (en) * | 2018-05-18 | 2018-10-16 | 宜昌金信化工有限公司 | A kind of cleaning method of glycine production waste water |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102020389A (en) * | 2010-11-19 | 2011-04-20 | 杭州蓝然环境技术有限公司 | Process for recycling ammonium chloride waste water |
| CN102107978A (en) * | 2010-12-23 | 2011-06-29 | 惠州市奥美特环境科技有限公司 | Method for resource utilization and innocent treatment of etching waste liquid containing copper in circuit board industry |
| CA2913308A1 (en) * | 2013-05-23 | 2014-11-27 | Veolia Water Solutions & Technologies Support | Wastewater treatment processes employing high rate chemical softening systems |
| CN104355474A (en) * | 2014-11-07 | 2015-02-18 | 清远市中宇环保实业有限公司 | Technique for extracting copper ions from industrial wastewater |
-
2015
- 2015-07-02 CN CN201510380439.6A patent/CN104944668B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102020389A (en) * | 2010-11-19 | 2011-04-20 | 杭州蓝然环境技术有限公司 | Process for recycling ammonium chloride waste water |
| CN102107978A (en) * | 2010-12-23 | 2011-06-29 | 惠州市奥美特环境科技有限公司 | Method for resource utilization and innocent treatment of etching waste liquid containing copper in circuit board industry |
| CA2913308A1 (en) * | 2013-05-23 | 2014-11-27 | Veolia Water Solutions & Technologies Support | Wastewater treatment processes employing high rate chemical softening systems |
| CN104355474A (en) * | 2014-11-07 | 2015-02-18 | 清远市中宇环保实业有限公司 | Technique for extracting copper ions from industrial wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 丁润发: "三效热泵蒸发工艺在含氨废水处理中的应用及经济分析", 《广东化工》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105601014A (en) * | 2015-12-28 | 2016-05-25 | 江苏瑞达环保科技有限公司 | Ammonia-nitrogen wastewater resourceful treatment system and treatment method of ammonia-nitrogen wastewater resourceful treatment system |
| CN105601014B (en) * | 2015-12-28 | 2018-01-12 | 江苏瑞达环保科技有限公司 | A kind of ammonia nitrogen waste water recycling treatment system and its processing method |
| CN107586958A (en) * | 2017-08-25 | 2018-01-16 | 金川集团股份有限公司 | A kind of method of ammonium root recycling in waste water of noble metal containing ammonium |
| CN108658374A (en) * | 2018-05-18 | 2018-10-16 | 宜昌金信化工有限公司 | A kind of cleaning method of glycine production waste water |
| CN108658374B (en) * | 2018-05-18 | 2021-06-08 | 湖北泰盛化工有限公司 | Clean treatment method of glycine production wastewater |
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| CN104944668B (en) | 2017-04-12 |
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