CN112239300A - Ammonium thiosulfate wastewater treatment method - Google Patents

Ammonium thiosulfate wastewater treatment method Download PDF

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Publication number
CN112239300A
CN112239300A CN202011479375.2A CN202011479375A CN112239300A CN 112239300 A CN112239300 A CN 112239300A CN 202011479375 A CN202011479375 A CN 202011479375A CN 112239300 A CN112239300 A CN 112239300A
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wastewater
ammonium thiosulfate
toc
treating
oxidant
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陆平
李霞
刘海良
贾楠楠
何秀萍
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Kemai Chemical Co Ltd
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Kemai Chemical Co Ltd
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    • 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
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/285—Treatment of water, waste water, or sewage by sorption using synthetic organic sorbents
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • 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
    • C02F2101/101—Sulfur 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
    • C02F2101/10—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
    • C02F2303/00—Specific treatment goals
    • C02F2303/16—Regeneration of sorbents, filters

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)

Abstract

The invention belongs to the field of wastewater treatment, and particularly relates to a method for treating ammonium thiosulfate wastewater, which comprises the following steps: evaporating the ammonium thiosulfate wastewater by MVR to obtain high TOC ammonium thiosulfate mother liquor; oxidizing the mother liquor with an oxidant; filtering the oxidized wastewater and analyzing the composition of solid residues; the content of the sulfur in the solid residue is higher than 95 percent, and the solid residue can be directly put into production procedures for recycling as the sulfur; and (3) adsorbing the oxidized and filtered wastewater by using large-aperture resin, and merging the mother liquor adsorbed by the large-aperture resin into raw water to enter an MVR evaporation system to obtain industrial salt and production reuse water. The treatment process has the advantages of complete treatment process, effective treatment of all wastes, low treatment cost and low process risk, and is a treatment scheme for effectively treating the ammonium thiosulfate wastewater.

Description

Ammonium thiosulfate wastewater treatment method
Technical Field
The invention belongs to the field of wastewater treatment, and particularly relates to a method for treating ammonium thiosulfate wastewater.
Background
The production process of a rubber accelerator DPG (hereinafter referred to as accelerator D) produces a large amount of ammonium thiosulfate wastewater, and the current treatment scheme of the wastewater comprises the following 4 types:
firstly), adjusting the pH value, filtering, and then entering an evaporation link (MVR, multiple-effect) to obtain high-TOC ammonium thiosulfate mother liquor and production reuse water, wherein the high-TOC ammonium thiosulfate mother liquor is evaporated to dryness to obtain ammonium thiosulfate waste salt.
Secondly), coagulating, aerating and precipitating by adopting a large proportion of lime ferrous sulfate, filtering, leading clear liquid to enter an evaporation link (MVR, multiple effects) to obtain mother liquid and production reuse water, mixing the mother liquid into raw water, continuing coagulating, aerating and precipitating, and finally achieving circulating treatment.
Thirdly), adding ammonium thiosulfate into the D promoting wastewater, reducing the solubility of organic matters in the wastewater through salting out, separating the organic matters from the wastewater, and then performing an evaporation link to obtain industrial salt and production reuse water.
Fourthly) a high-temperature high-pressure wet oxidation technology, generally oxidizing the waste water at the temperature of 250-300 ℃ and under the pressure of 6-8MPa, and evaporating the effluent to obtain finished industrial salt and production reuse water.
Aiming at the scheme I), the energy consumption of the high TOC mother liquor in the evaporation process is extremely high, salt is difficult to produce in the evaporation process, the produced salt is ammonium thiosulfate and ammonium sulfate mixed salt which cannot be sold as industrial products, and the solid waste is difficult to treat in the later period, so that the cost is extremely high.
Aiming at the scheme II), a large amount of black calcium salt solid cost is generated, the solid waste belongs to dangerous waste, no proper treatment scheme exists at present, and the completely harmless treatment of the waste water cannot be realized.
Aiming at the third scheme), the salting-out process has a process of periodically discharging liquid and separately treating the liquid because organic matters cannot be completely separated out from the wastewater and the organic matters with good water solubility can be accumulated in the long-term circulation process.
Aiming at the scheme IV), the wet oxidation process has low energy consumption for treating wastewater, can balance heating energy consumption in the organic matter oxidation process, can completely treat wastewater and salt in a harmless way, has the defects of high one-time investment of devices, high maintenance cost, high safety risk and the like when the devices are operated in an ultrahigh-temperature and high-pressure state.
In conclusion, the traditional ammonium thiosulfate wastewater treatment process has obvious defects in aspects of product yield device investment, maintenance cost, process integrity, post-treatment and the like, and has the problems of high safety risk, high investment cost and the like in the actual treatment process.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provides a method for treating ammonium thiosulfate wastewater.
In order to achieve the purpose, the invention adopts the technical scheme that:
a method for treating ammonium thiosulfate wastewater comprises the following steps:
evaporating ammonium thiosulfate wastewater through MVR to obtain high-TOC ammonium thiosulfate mother liquor;
step (2), oxidizing the mother liquor and an oxidant;
step (3), filtering the oxidized wastewater and analyzing the composition of solid residues; the content of the sulfur in the solid residue is higher than 95 percent, and the solid residue can be directly put into production procedures for recycling as the sulfur;
absorbing the oxidized and filtered wastewater by using large-aperture resin;
and (5) merging the mother liquor after the adsorption of the large-aperture resin into raw water to enter an MVR evaporation system to obtain industrial salt and production reuse water.
Preferably, in the ammonium thiosulfate wastewater in the step (1), COD is more than 20000, and TOC is more than 5000; COD in the high-TOC ammonium thiosulfate mother liquor is 80000, and TOC is 10000.
Preferably, the COD of the wastewater after oxidation in the step (4) is less than 15000, and the TOC is less than 7000; the TOC after adsorption through the large-aperture resin is reduced to below 500.
The oxidant in the step (2) is air, oxygen or hydrogen peroxide.
When the oxidant is air, the air pressure is selected to be 0.6-1.5MPa, and the temperature is 60-150 ℃ for oxidation; when the oxidant is oxygen, the oxygen pressure is selected to be 0.6-1.5MPa, and the temperature is 60-150 ℃ for oxidation; when the oxidant is hydrogen peroxide, the feeding ratio of the hydrogen peroxide is 2-10%, and the temperature is 60-150 ℃ for oxidation.
When the oxidant is air, the air pressure is 0.6-1.5MPa, and the reaction temperature is 60-150 ℃; when the oxidant is oxygen, the oxygen pressure is 0.6-1.5MPa, and the reaction temperature is 60-150 ℃; when the oxidant is hydrogen peroxide, the feeding ratio of the hydrogen peroxide is 2-10%, and the reaction temperature is 60-150 ℃.
The waste water adsorption airspeed in the step (4) is 1-10h-1The preferred adsorption space velocity is 2-5h-1。
And (3) carrying out solvent backwashing on the large-aperture resin for reuse. The solvent in the solvent backwashing is selected from one of acetone, isopropanol or methanol; carrying out multi-stage water washing on the backwashed solvent to recover the solvent, and evaporating to obtain solid waste residues; and (4) putting the solid waste into a burning system for burning, and performing harmless treatment on the solid waste.
Compared with the prior art, the invention has the beneficial effects that:
the process of treating waste water containing ammonium thiosulfate includes evaporating to obtain mother liquid with high TOC content and reuse water, simple oxidation of the mother liquid, adsorption with large pore size resin, circular feeding to raw water system to obtain industrial salt product and reuse water, and burning the solid waste produced in the resin adsorption process in burning system. The process adopts simple oxidation, avoids the problem of high equipment investment caused by high-temperature and high-pressure wet oxidation, reduces the risk of the process, simultaneously makes industrial mixed salt into a single ammonium sulfate component through the oxidation process, reaches the standard of industrial salt, reduces the output of solid waste, and can sell the byproduct ammonium sulfate as a commodity. In addition, the process combines a large-aperture resin adsorption technology to effectively separate soluble organic matters from the wastewater, so that the problem of organic matter circulating accumulation in the wastewater evaporation process is properly solved, and after the organic matter outlet is increased, the energy consumption in the evaporation process is reduced, and the equipment risk is reduced. And finally, from the view of process integrity, the treatment process has the advantages of complete treatment process of the whole process, effective treatment of all wastes, low treatment cost and low process risk, and is a treatment scheme for effectively treating the ammonium thiosulfate wastewater.
Compared with the reported technology, the method has the following advantages:
1. the equipment investment cost is low once, and the equipment is normal pressure equipment except the oxidation reaction kettle, and compared with the traditional wet oxidation equipment, the reaction severity is low, and the oxidation reaction kettle adopts medium temperature and medium pressure equipment, so that the equipment requirement is low, the safety is high, and the maintenance is simple.
2. The large-aperture resin adsorption technology is combined, the COD outlet problem in the wastewater is solved, and the core problems that the evaporation energy consumption is increased and the evaporation can not be circularly carried out due to COD accumulation in the evaporation process are solved.
3. The process integrity is good, the subsequent treatment of all solid-liquid waste residues in the wastewater is solved by combining the incineration mode, and the complete harmless treatment of the wastewater is achieved.
4. The mixed salt after the previous treatment means is changed into single industrial salt, the problem of salt export is solved, and the whole treatment chain is opened.
5. New solid waste residue is not generated in the treatment process, the treatment process is economical and feasible, and the environmental protection risk of the original treatment means is reduced.
6. The reaction kettle and the adsorption tower which are related by the invention are normal pressure equipment except the medium-temperature oxidation reaction kettle, and basically have no environmental protection and process risk.
Detailed Description
In order to make those skilled in the art better understand the technical solution of the present invention, the following provides a detailed description of the present invention with reference to the embodiments.
Example (b): the embodiment provides a method for treating ammonium thiosulfate wastewater, which comprises the following steps:
(1) evaporating ammonium thiosulfate wastewater (COD is more than 20000, TOC is more than 5000) by MVR to obtain high-TOC ammonium thiosulfate mother liquor (COD is more than 80000, TOC is more than 10000);
(2) 600 g of high TOC ammonium thiosulfate mother liquor is oxidized by oxygen, the reaction pressure of the treatment conditions is 0.6MPa/0.8MPa/1.0MPa/1.2MPa/1.5MPa respectively, and the reaction is carried out for 2 hours at the reaction temperature of 120 ℃. Table 1 shows the COD and TOC values of wastewater and the solid waste mass obtained by treating oxygen at different pressures according to different examples; obtaining treated mother liquor and solid residues, wherein analytical data shows that the analytical composition of the solid residues is less than 95% of sulfur.
TABLE 1
Examples Oxygen oxidation pressure COD TOC Mass of solid waste (g)
Blank space Raw water 83900 13800
Example 1 0.6MPa 68700 11500 2.1
Example 2 0.8MPa 25200 8890 5.2
Example 3 1.0MPa 15300 6500 9.5
Example 4 1.2MPa 13900 5100 12.3
Example 5 1.5MPa 11500 3700 13.5
(3) 600 g of high-TOC ammonium thiosulfate mother liquor is oxidized by air, the reaction pressure of the treatment conditions is 0.6MPa/0.8MPa/1.0MPa/1.2MPa/1.5MPa, the reaction is carried out for 2 hours at the reaction temperature of 120 ℃, and the treated mother liquor and solid residues are obtained, and the data are analyzed. Table 2 shows the COD and TOC values of the wastewater and the solid waste mass obtained by treating air at different pressures according to different examples; the analytical composition differences of the solid waste residue are less than 95 percent of sulfur.
TABLE 2
Examples Air oxidation pressure COD TOC Mass of solid waste (g)
Blank space Raw water 81500 12300
Example 6 0.6MPa 71500 11900 1.8
Example 7 0.8MPa 38500 9560 4.3
Example 8 1.0MPa 21500 7700 7.3
Example 9 1.2MPa 14500 6470 9.8
Example 10 1.5MPa 12320 5050 12.5
(4) Oxidizing 600 g of high-TOC ammonium thiosulfate mother liquor by using hydrogen peroxide, reacting for 2 hours at the reaction temperature of 120 ℃ under the treatment condition of 2%/4%/5%/7%/10%, and obtaining treated mother liquor and solid residues, and analyzing data. Table 3 shows the COD and TOC values of the wastewater and the solid waste mass obtained by treating the wastewater with different amounts of hydrogen peroxide according to different embodiments; the analytical composition differences of the solid waste residue are less than 95 percent of sulfur.
TABLE 3
Examples Hydrogen peroxide oxidation batch COD TOC Mass of solid waste (g)
Blank space Raw water 82700 13100
Example 11 0.02 76150 12500 0.5
Example 12 0.04 71200 11700 2
Example 13 0.05 45300 10580 3.5
Example 14 0.07 16800 6790 9.8
Example 15 0.1 11300 4500 12.4
Analyzing the above data in combination with the treatment effect of investment cost, preferably selecting oxygen as oxidant and pressure of 1.0MPa
(5) Oxidizing 600 g of high-TOC ammonium thiosulfate mother liquor by oxygen, reacting for 2 hours under the treatment conditions of the reaction pressure of 1.0MPa and the reaction temperature of 60/90/120/150 ℃ to obtain treated mother liquor and solid residues, and analyzing data; table 4 shows the COD and TOC values of the wastewater and the solid waste mass obtained from the treatments at different temperatures; the analytical composition differences of the solid waste residue are less than 95 percent of sulfur.
TABLE 4
Examples Temperature of oxygen oxidation COD TOC Mass of solid waste (g)
Blank space Raw water 83900 13800
Example 16 60 77800 13200 0.5
Example 17 90 33700 11500 4.8
Example 18 120 15300 6500 9.5
Example 19 150 11500 4500 11.8
The above data are analyzed in combination with the treatment effect of investment cost, oxygen is preferably used as the oxidant, the pressure is preferably 1.0MPa, and the temperature is preferably 120 ℃.
(6) 600 g of high-TOC ammonium thiosulfate mother liquor is oxidized by oxygen, and reacts for 1/2/3/4 hours under the treatment conditions of the reaction pressure of 1.0MPa and the reaction temperature of 120 ℃ to obtain the treated mother liquor and solid residue, and the analysis data is obtained. Table 5 shows the COD and TOC values of the wastewater and the solid waste mass obtained at different reaction times corresponding to the reaction times; the analytical composition differences of the solid waste residue are less than 95 percent of sulfur.
TABLE 5
Examples Oxygen oxidation time (h) COD TOC Mass of solid waste (g)
Blank space Raw water 83900 13800
Example 20 1 25800 7800 7.5
Example 21 2 15300 6500 9.5
Example 22 3 14800 5800 9.8
Example 23 4 14200 5500 10.8
The above data are analyzed in combination with the investment cost treatment effect, preferably oxygen as the oxidant, preferably at a pressure of 1.0MPa, preferably at a temperature of 120 ℃ and preferably for a reaction time of 2 hours.
(7) Adsorbing the oxidized large-aperture resin and inspecting the quality of the discharged water, wherein the water inlet speed is 1h-1The water quality was examined every 2 volumes of water (resin volume). Table 6 shows the effluent COD and TOC values for different resin volumes for different examples, and analytical data 8 resin volume water required backwashing of the resin.
TABLE 6
Examples Resin adsorption effluent COD TOC
Blank space Raw water 15300 6500
Example 24 1 3500 350
Example 25 2 4100 370
Example 26 3 4300 450
Example 27 4 5500 660
(8) After acetone is subjected to reverse washing, absorbing the oxidized effluent by macroporous resin, then inspecting the effluent quality, wherein the water inlet speed is 1h-1, and the effluent quality is inspected once every 2 volumes of water (resin volume). Table 7 shows the effluent COD and TOC values for the various examples after the backwash, and the analytical data show that the resin after the backwash achieves regeneration.
TABLE 7
Examples Resin adsorption effluent COD TOC
Blank space Raw water 15300 6500
Example 28 1 3480 340
Example 29 2 4200 385
Example 30 3 4450 475
Example 31 4 5700 690
(9) The salt water obtained in example 29 was evaporated to salt by MVR and analyzed by GB/T535-1995 ammonium sulfate analysis method; the analysis data of the obtained salt is shown in Table 8, and the result shows that the mixed salt is changed into single industrial salt and can be directly used for industrial production.
TABLE 8
Appearance of the product White crystal
Nitrogen (N) content (on a dry basis)% 20.6
Water content (H2O)% 0.9
Free acid (H2 SO 4)% 0.15
Iron content% Not detected out
Arsenic content% Not detected out
Heavy metal (calculated as Pb)% Not detected out
Content of water-insoluble matter 0.008
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.

Claims (10)

1. The method for treating the ammonium thiosulfate wastewater is characterized by comprising the following steps of:
evaporating ammonium thiosulfate wastewater through MVR to obtain high-TOC ammonium thiosulfate mother liquor;
step (2), oxidizing the mother liquor and an oxidant;
step (3), filtering the oxidized wastewater and analyzing the composition of solid residues; the content of the sulfur in the solid residue is higher than 95 percent, and the solid residue can be directly put into production procedures for recycling as the sulfur;
absorbing the oxidized and filtered wastewater by using large-aperture resin;
and (5) merging the mother liquor after the adsorption of the large-aperture resin into raw water to enter an MVR evaporation system to obtain industrial salt and production reuse water.
2. The method for treating ammonium thiosulfate wastewater in accordance with claim 1, characterized in that in the ammonium thiosulfate wastewater in the step (1), COD is >20000, TOC is > 5000; COD in the high-TOC ammonium thiosulfate mother liquor is 80000, and TOC is 10000.
3. The ammonium thiosulfate wastewater treatment method according to claim 1, characterized in that the oxidized wastewater in step (4) has COD <15000, TOC < 7000; the TOC after adsorption through the large-aperture resin is reduced to below 500.
4. The method for treating the ammonium thiosulfate wastewater in the claim 1 is characterized in that the oxidant in the step (2) is air, oxygen or hydrogen peroxide.
5. The ammonium thiosulfate wastewater treatment method of claim 4, characterized in that when the oxidizing agent is air, the air pressure is 0.6-1.5MPa, and the reaction temperature is 60-150 ℃; when the oxidant is oxygen, the oxygen pressure is 0.6-1.5MPa, and the reaction temperature is 60-150 ℃; when the oxidant is hydrogen peroxide, the feeding ratio of the hydrogen peroxide is 2-10%, and the reaction temperature is 60-150 ℃.
6. The method for treating ammonium thiosulfate wastewater as claimed in claim 4, wherein when the oxidant is air, the air pressure is selected from 0.8-1.0MPa, and the temperature is 100-120 ℃ for oxidation; when the oxidant is oxygen, the oxygen pressure is selected to be 0.8-1.0MPa, and the temperature is 100-; when the oxidant is hydrogen peroxide, the feeding ratio of the hydrogen peroxide is 3-5%, and the temperature is 100 ℃ and 120 ℃ for oxidation.
7. The method for treating ammonium thiosulfate wastewater in claim 1, characterized in that the space velocity of wastewater adsorption in step (4) is 1-10h-1。
8. The method for treating ammonium thiosulfate wastewater according to claim 1, characterized in that the large-pore-diameter resin is mechanically used for solvent backwashing.
9. The method for treating ammonium thiosulfate wastewater as claimed in claim 8, wherein the solvent in the solvent backwashing is selected from one of acetone, isopropanol and methanol.
10. The method for treating ammonium thiosulfate wastewater according to claim 8, characterized in that the backwashed solvent is washed with water in multiple stages to recover the solvent, and the solvent is evaporated to obtain solid waste residues; and (4) putting the solid waste into a burning system for burning, and performing harmless treatment on the solid waste.
CN202011479375.2A 2020-12-16 2020-12-16 Ammonium thiosulfate wastewater treatment method Pending CN112239300A (en)

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CN105073646A (en) * 2013-03-12 2015-11-18 3M创新有限公司 Removal of chlorine and/or chloramine from aqueous solutions
CN105330082A (en) * 2015-12-09 2016-02-17 南京环保产业创新中心有限公司 Treatment method for 4-methyl-2-benzothiazolehydrazine production wastewater
CN109399850A (en) * 2018-10-24 2019-03-01 科迈化工股份有限公司 Rubber accelerator DPG waste water treatment process

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6258279B1 (en) * 1998-04-24 2001-07-10 Nalco Chemical Company Hydrophilic cationic dispersion polymer for paper mill color removal
CN105073646A (en) * 2013-03-12 2015-11-18 3M创新有限公司 Removal of chlorine and/or chloramine from aqueous solutions
CN105330082A (en) * 2015-12-09 2016-02-17 南京环保产业创新中心有限公司 Treatment method for 4-methyl-2-benzothiazolehydrazine production wastewater
CN109399850A (en) * 2018-10-24 2019-03-01 科迈化工股份有限公司 Rubber accelerator DPG waste water treatment process

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
王芳: ""焦炉煤气脱硫废液资源化处理研究"", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 *

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Application publication date: 20210119