CN1781859A - Method for treating waste water from meta dinitro benzene production - Google Patents
Method for treating waste water from meta dinitro benzene production Download PDFInfo
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Abstract
The process of treating waste water from m-dinitrobenzene production includes the following main steps: regulating acidity of the waste water, standing, filtering and adsorbing in macroporous resin filling adsorption tower; stopping adsorption after reaching the first falloff point and desorption regenerating with sodium hydroxide aqua as desorbent; regulating acidity for the second time and adsorbing in macroporous resin filling adsorption tower for the second time; stopping adsorption after reaching the second falloff point and desorption regenerating with sodium hydroxide aqua as desorbent; and regulating acidity, decolorizing in adsorption tower filled with active carbon to obtain colorless transparent water. The said process can treat waste water from m-dinitrobenzene production to exhaust standard, and the adsorption resin may be regenerated for reuse.
Description
One, technical field
The present invention relates to the method for wastewater treatment that produced in a kind of Meta-dinitrobenzene production process, more particularly, a kind of exactly method of from waste water from meta dinitro benzene production, isolating nitrobenzene-sulfonic acid salt.
Two, background technology
Meta-dinitrobenzene mainly is used as the intermediate of dyestuff, pigment and other organic syntheses.The waste water COD of discharging during it is produced
CrUp to 10000～15000mg/L, contain the organic pollutant and the Na such as Meta-dinitrobenzene of o-nitrobenzene sulfonic acid sodium, paranitrobenzenesulfonic acid sodium, minute quantity
2SO
3, NaNO
2Deng inorganic pollutant.Because this strand waste water saltiness height, toxicity is bigger, adopts methods such as conventional biochemistry, chemical oxidation to be difficult to prove effective, and simultaneously because the main component nitro-compound in the waste water belongs to strong carcinogen, enters water body and will cause HUMAN HEALTH and seriously influence.A large amount of Meta-dinitrobenzene waste water is effectively administered at present, and this also certainly will seriously restrict the Sustainable development of Meta-dinitrobenzene manufacturing enterprise.
Three, summary of the invention
The purpose of this invention is to provide a kind of technical scheme, can remove the principal pollutant nitro-sulfonic acid salt in the waste water that is produced in the Meta-dinitrobenzene production process, effluent color dilution is up to standard behind activated carbon decolorizing again, COD
CrCan significantly reduce.
Technical scheme of the present invention is as follows:
A kind of treatment process of waste water from meta dinitro benzene production may further comprise the steps:
(A) will leave standstill filtration after the waste water from meta dinitro benzene production acid adjustment, remove suspended substance wherein;
(B) filtrate that step (A) is obtained is by being filled with the macroporous resin absorption tower, and absorption effluent is red solution;
(C) when absorption reaches first leakage point (as absorption effluent COD
CrBe first leakage point when reaching the 3000mg/L left and right sides) stop absorption, as desorbing agent, carry out desorption and regeneration with aqueous sodium hydroxide solution;
(D) with after the absorption effluent acid adjustment of (B) once more by being filled with the macroporous resin absorption tower, the nitrobenzene-sulfonic acid in the waste water optionally is adsorbed on the resin, absorption effluent is red solution;
(E) when absorption reaches second leakage point, stop absorption, as desorbing agent, carry out desorption and regeneration with aqueous sodium hydroxide solution;
(F) with after the absorption effluent acid adjustment of (D) by being filled with the adsorption tower of gac, to the waste water processing of decolouring, absorption effluent is a colourless transparent liquid.
In the step (A), waste water ph is adjusted to 1-4, leaves standstill 24-48h, and in the step (D), waste water ph is adjusted to 1-4, and the effect of absorption can be relatively good like this, says that from technique effect the more little corresponding effects of pH value is better, but can increase cost simultaneously.
Send burning outside or be used for the production coal water slurry after the sodium salt solution of the high nitrobenzene sulfonic acid that desorption gets off in step (C) and the step (E) concentrates with concentration kettle, light concentration desorption liquid is used to prepare the aqueous sodium hydroxide solution cover and is used for the next batch desorption manipulation and (is high density with what the sodium hydroxide solution desorption got off, will follow desorption with clear water after sodium hydroxide solution washes, what desorption got off is light concentration desorption liquid).Step (C) and (E) in, the sodium hydroxide weight percent concentration is 2%～10%, carries out desorption and regeneration at 35～55 ℃ with the flow of 0.5～2 resin bed volume per hour.
Macroporous resin in step (B) and the step (D) is to be the macroporous resin of basic framework with the polystyrene.These macroporous resins are ND-1507 complexing polymeric adsorbent, NDA-99 and NDA-88 complex function adsorption resin (Jiangsu Nanda Gede Environmental Protection Technology Co., Ltd's production) and D301 resin productions such as () Langfang, Hebei electric power resin processing plants preferably, also can be Amberlite IRA96, the IRA93 macroporous resin that U.S. Rohm Haas company produces.
Gac described in the step (F) can be coconut husk charcoal or carbo lignius, requires its methylene blue adsorptive value to be higher than 200mg/g, preferably coconut husk decoloration active carbon (the methylene blue adsorptive value is higher than 225mg/g).
In the step (B), 5～40 ℃ of filtrates that step (A) is obtained with the flow of 0.5～1.5 resin bed volume (BV) per hour by being filled with the macroporous resin absorption tower, upper prop liquid in the step (D) with the flow of 0.5～3 resin bed volume per hour by being filled with the macroporous resin absorption tower, the upper prop liquid in the step (F) with the flow of 1～5 active carbon bed volume per hour by being filled with the adsorption tower of gac.
Absorption reaches the second leakage point (COD
CrSurpassing 100mg/L or water outlet obviously has color to be second leakage point) time stop absorption, gac is carried out the wastewater treatment that high temperature regeneration is used for next batch.
Beneficial effect
The invention provides a kind of treatment process of waste water from meta dinitro benzene production, can handle the waste water of discharging effectively.By the present invention, waste water from meta dinitro benzene production can be realized qualified discharge, and the sodium salt solution of the high nitrobenzene sulfonic acid that the while desorption gets off also can re-use; The polymeric adsorbent regenerability is good, and is reusable.The present invention produces economic benefit again when producing environmental benefit.
Four, embodiment
Further specify the present invention by the following examples.
Embodiment 1:
(1) one-level absorption
20mL (about 14 gram) macropore complexing polymeric adsorbent NDA-1507 packed in the glass adsorption column of strap clamp cover, and (Φ 12 * 160mm).Waste water COD
CrBe 11000mg/L, add H
2SO
4Leave standstill 24h after regulating pH=1.5, after the filtration with it in 15 ± 5 ℃, by resin bed, treatment capacity is that 160mL/ criticizes with the flow of 20mL/h.After resin absorption, water outlet COD
CrBe 2150mg/L.
Adsorb when reaching first leakage point (as absorption effluent COD
CrBe first leakage point when reaching the 3000mg/L left and right sides) stop absorption, the 30mL6% aqueous sodium hydroxide solution under 45 ± 5 ℃ temperature, is carried out desorption with the flow following current of 5mL/h by resin bed.The high nitrobenzene sulfonate sodium solution that desorption gets off can send the system coal water slurry outside or concentrate after send incineration disposal outside.Light concentration desorption liquid is used to prepare the used aqueous sodium hydroxide solution of next batch desorption.
(2) secondary absorption
10mL (about 7 gram) macropore complexing polymeric adsorbent NDA-1507 packed in the glass adsorption column of strap clamp cover, and (Φ 12 * 160mm).Water inlet COD
CrBe 2150mg/L, add H
2SO
4Regulate behind the pH=1.5 it in 15 ± 5 ℃, by resin bed, treatment capacity is that 160mL/ criticizes with the flow of 20mL/h.After resin absorption, water outlet COD
CrBe 650mg/L.
(COD when absorption reaches second leakage point
CrSurpassing 100mg/L or water outlet obviously has color to be second leakage point) time stop absorption, with the 15mL weight percent be 6% aqueous sodium hydroxide solution under 45 ± 5 ℃ temperature, carry out desorption with the flow following current of 5mL/h by resin bed.The high nitrobenzene sulfonate sodium solution that desorption gets off can send the system coal water slurry outside or concentrate after send incineration disposal outside.Light concentration desorption liquid is used to prepare the used aqueous sodium hydroxide solution of next batch desorption.
(3) activated carbon decolorizing
10mL (about 5 gram) cocoanut active charcoal packed in the glass adsorption column of strap clamp cover, and (Φ 12 * 160mm).Water inlet COD
CrBe 650mg/L, add H
2SO
4Regulate behind the pH=3 it in 15 ± 5 ℃, by resin bed, treatment capacity is that 160mL/ criticizes with the flow of 30mL/h.After charcoal absorption, water outlet COD
CrBe 85mg/L.
Embodiment 2:
(1) one-level absorption
100mL (about 700 gram) macropore complexing polymeric adsorbent NDA-1507 packed in the glass adsorption column of strap clamp cover, and (Φ 32 * 260mm).Waste water COD
CrBe 15000mg/L, add H
2SO
4Leave standstill 48h after regulating pH=1, after the filtration with it in 15 ± 5 ℃, by resin bed, treatment capacity is that 700mL/ criticizes with the flow of 120mL/h.After resin absorption, water outlet COD
CrBe 2560mg/L.
100mL 10% aqueous sodium hydroxide solution under 35 ± 5 ℃ temperature, is carried out desorption with the flow following current of 50mL/h by resin bed.The high nitrobenzene sulfonate sodium solution that desorption gets off can send the system coal water slurry outside or concentrate after send incineration disposal outside.Light concentration desorption liquid is used to prepare the used aqueous sodium hydroxide solution of next batch desorption.
(2) secondary absorption
50mL (about 350 gram) macropore complexing polymeric adsorbent NDA-1507 packed in the glass adsorption column of strap clamp cover, and (Φ 32 * 260mm).Water inlet COD
CrBe 2560mg/L, add H
2SO
4Regulate behind the pH=1 it in 15 ± 5 ℃, by resin bed, treatment capacity is that 700mL/ criticizes with the flow of 100mL/h.After resin absorption, water outlet COD
CrBe 820mg/L.
The 50mL10% aqueous sodium hydroxide solution under 35 ± 5 ℃ temperature, is carried out desorption with the flow following current of 25mL/h by resin bed.The high nitrobenzene sulfonate sodium solution that desorption gets off can send the system coal water slurry outside or concentrate after send incineration disposal outside.Light concentration desorption liquid is used to prepare the used aqueous sodium hydroxide solution of next batch desorption.
(3) activated carbon decolorizing
50mL (about 25 gram) cocoanut active charcoal packed in the glass adsorption column of strap clamp cover, and (Φ 32 * 260mm).Water inlet COD
CrBe 820mg/L, add H
2SO
4Regulate behind the pH=3 it in 15 ± 5 ℃, by resin bed, treatment capacity is that 700mL/ criticizes with the flow of 100mL/h.After charcoal absorption, water outlet COD
CrBe 90mg/L.
Embodiment 3:
(1) one-level absorption
1000mL (about 7000 gram) macropore complexing polymeric adsorbent NDA-1507 packed in the glass adsorption column of strap clamp cover, and (Φ 70 * 500mm).Waste water COD
CrBe 13000mg/L, add H
2SO
4Leave standstill 36h after regulating pH=4, after the filtration with it in 15 ± 5 ℃, by resin bed, treatment capacity is that 6000mL/ criticizes with the flow of 500mL/h.After resin absorption, water outlet COD
CrBe 1860mg/L.
The 1500mL6% aqueous sodium hydroxide solution under 40 ± 5 ℃ temperature, is carried out desorption with the flow following current of 1500mL/h by resin bed.The high nitrobenzene sulfonate sodium solution that desorption gets off can send the system coal water slurry outside or concentrate after send incineration disposal outside.Light concentration desorption liquid is used to prepare the used aqueous sodium hydroxide solution of next batch desorption.
(2) secondary absorption
500mL (about 3500 gram) macropore complexing polymeric adsorbent NDA-1507 packed in the glass adsorption column of strap clamp cover, and (Φ 70 * 500mm).Water inlet COD
CrBe 1860mg/L, add H
2SO
4Regulate behind the pH=1.5 it in 15 ± 5 ℃, by resin bed, treatment capacity is that 6000mL/ criticizes with the flow of 1500mL/h.After resin absorption, water outlet COD
CrBe 660mg/L.
The 750mL6% aqueous sodium hydroxide solution under 40 ± 5 ℃ temperature, is carried out desorption with the flow following current of 500mL/h by resin bed.The high nitrobenzene sulfonate sodium solution that desorption gets off can send the system coal water slurry outside or concentrate after send incineration disposal outside.Light concentration desorption liquid is used to prepare the used aqueous sodium hydroxide solution of next batch desorption.
(3) activated carbon decolorizing
100mL (about 50 gram) cocoanut active charcoal packed in the glass adsorption column of strap clamp cover, and (Φ 32 * 260mm).Water inlet COD
CrBe 660mg/L, add H
2SO
4Regulate behind the pH=3 it in 15 ± 5 ℃, by resin bed, treatment capacity is that 2000mL/ criticizes with the flow of 100mL/h.After charcoal absorption, water outlet COD
CrBe 78mg/L.
Embodiment 4:
(1) one-level absorption
Select that three specifications are identical, material is 316L stainless steel adsorption tower for use (Φ 550 * 3500mm), compile Shang number be respectively I, II and III, every tower loads 350 kilograms of (about 0.5m of NDA-1507 polymeric adsorbent
3).Waste water COD
CrBe 10000mg/L, add H
2SO
4Leave standstill 24h after regulating pH=1.2, after the filtration with it in 20 ± 5 ℃, with 0.5m
3The flow of/h is squeezed into adsorption tower with pump, and the mode of I, II tower double-column in series following current absorption is adopted in absorption, and treatment capacity is 4m
3/ batch.After resin absorption, water outlet COD
CrBe 1950mg/L.
To adsorb 4m
3The first post I adsorption tower of waste water breaks away from absorption system and carries out desorption manipulation; And the next batch adsorption operations changes II, the series operation of III tower into, post headed by the II tower becomes.
Earlier raffinate in the I adsorption tower is drained, again with 0.75m
32% aqueous sodium hydroxide solution is under 35 ± 5 ℃ temperature, with 0.25m
3The flow following current of/h is carried out desorption by resin bed.The high nitrobenzene sulfonate sodium solution that desorption gets off can send the system coal water slurry outside or concentrate after send incineration disposal outside.Light concentration desorption liquid is used to prepare the used aqueous sodium hydroxide solution of next batch desorption.
I adsorption tower after desorption finishes will be as the stern post of the 3rd batch of adsorption operations.Can guarantee that by the present invention whole waste water treatment device moves continuously.
(2) secondary absorption
Select that three specifications are identical, material is 316L stainless steel adsorption tower for use (Φ 450 * 3000mm), compile Shang number be respectively I, II and III, every tower loads 200 kilograms of (about 0.3m of NDA-1507 polymeric adsorbent
3).Water inlet COD
CrBe 1950mg/L, add H
2SO
4Regulate behind the pH=1.2 it in 20 ± 5 ℃, with 0.6m
3The flow of/h is squeezed into adsorption tower with pump, and the mode of I, II tower double-column in series following current absorption is adopted in absorption, and treatment capacity is 4m
3/ batch.After resin absorption, water outlet COD
CrBe 800mg/L.
To adsorb 4m
3The first post I adsorption tower of waste water breaks away from absorption system and carries out desorption manipulation; And the next batch adsorption operations changes II, the series operation of III tower into, post headed by the II tower becomes.
Earlier raffinate in the I adsorption tower is drained, again with 0.6m
36% aqueous sodium hydroxide solution is under 35 ± 5 ℃ temperature, with 0.25m
3The flow following current of/h is carried out desorption by resin bed.The high nitrobenzene sulfonate sodium solution that desorption gets off can send the system coal water slurry outside or concentrate after send incineration disposal outside.Light concentration desorption liquid is used to prepare the used aqueous sodium hydroxide solution of next batch desorption.
I adsorption tower after desorption finishes will be as the stern post of the 3rd batch of adsorption operations.Can guarantee that by the present invention whole waste water treatment device moves continuously.
(3) activated carbon decolorizing
Select that three specifications are identical, material is 316L stainless steel adsorption tower for use (Φ 250 * 2000mm), compile Shang number be respectively I, II and III, every tower loads 100 kilograms of (about 0.2m of cocoanut active charcoal
3).Water inlet COD
CrBe 800mg/L, add H
2SO
4Regulate behind the pH=3 it in 20 ± 5 ℃, with 0.6m
3The flow of/h is squeezed into adsorption tower with pump, and the mode of I, II tower double-column in series following current absorption is adopted in absorption, and treatment capacity is 4m
3/ batch.After charcoal absorption, water outlet COD
CrBe 86mg/L.
To adsorb 4m
3The first post I adsorption tower raffinate of waste water drains, and takes out gac thermal regeneration wherein then
After reinstall this tower; And the next batch adsorption operations changes II, the series operation of III tower into, post headed by the II tower becomes.
I adsorption tower behind the regeneration ending will be as the stern post of the 3rd batch of adsorption operations.Can guarantee that by the present invention whole waste water treatment device moves continuously.
Embodiment 5
The elementary operation condition is with embodiment 3, just changes service temperature (temperature range is controlled at 5～50 ℃), (0.5～3BV) tests the filtrate flow velocity, and last effluent quality still can reach COD
CrLess than 100mg/L.
Embodiment 6
Change the NDA-1507 resin among the embodiment 1 domestic resins such as into NDA-99, NDA-88, NDA-100 and D301, or resin and macroporous weak such as U.S. AmberliteIRA93, IRA96, other operational conditions remain unchanged, except that every batch processing volume and absorption effluent water quality decreased, other effects substantially roughly the same.
Claims (10)
1. the treatment process of a waste water from meta dinitro benzene production is characterized in that it may further comprise the steps:
(A) will leave standstill filtration after the waste water from meta dinitro benzene production acid adjustment, remove suspended substance wherein;
(B) filtrate that step (A) is obtained is by being filled with the macroporous resin absorption tower, and absorption effluent is red solution;
(C) when absorption reaches first leakage point, stop absorption, as desorbing agent, carry out desorption and regeneration with aqueous sodium hydroxide solution;
(D) with after the absorption effluent acid adjustment of (B) once more by being filled with the macroporous resin absorption tower, the nitrobenzene-sulfonic acid in the waste water optionally is adsorbed on the resin, absorption effluent is red solution;
(E) when absorption reaches second leakage point, stop absorption, as desorbing agent, carry out desorption and regeneration with aqueous sodium hydroxide solution;
(F) with after the absorption effluent acid adjustment of (D) by being filled with the adsorption tower of gac, to the waste water processing of decolouring, absorption effluent is a colourless transparent liquid.
2. the treatment process of a kind of waste water from meta dinitro benzene production according to claim 1, send outside after the sodium salt solution that it is characterized in that high nitrobenzene sulfonic acid that desorption in step (C) and the step (E) is got off concentrates with concentration kettle and burn or be used for the production coal water slurry, light concentration desorption liquid is used to prepare the aqueous sodium hydroxide solution cover and is used for the next batch desorption manipulation.
3. the treatment process of a kind of waste water from meta dinitro benzene production according to claim 2 is characterized in that the macroporous resin in step (B) and the step (D) is to be the macroporous resin of basic framework with the polystyrene.
4. the treatment process of a kind of waste water from meta dinitro benzene production according to claim 3 is characterized in that the gac in the step (F) is the coconut husk decoloration active carbon.
5. the treatment process of a kind of waste water from meta dinitro benzene production according to claim 3, it is characterized in that in the step (B), 5～40 ℃ of filtrates that step (A) is obtained with the flow of 0.5～1.5 resin bed volume per hour by being filled with the macroporous resin absorption tower, upper prop liquid in the step (D) with the flow of 0.5～3 resin bed volume per hour by being filled with the macroporous resin absorption tower, the upper prop liquid in the step (F) with the flow of 1～5 active carbon bed volume per hour by being filled with the adsorption tower of gac.
6. the treatment process of a kind of waste water from meta dinitro benzene production according to claim 5 is characterized in that waste water ph is adjusted to 1-4, leaves standstill 24-48h in the step (A), and in the step (D), waste water ph is adjusted to 1-4.
7. according to the treatment process of the described waste water from meta dinitro benzene production of claim 4～6, it is characterized in that: step (C) and (E) in, the sodium hydroxide weight percent concentration is 2%～10%, carries out desorption and regeneration at 35～55 ℃ with the flow of 0.5～2 resin bed volume per hour.
8. according to the treatment process of the waste water from meta dinitro benzene production described in the claim 4～6, it is characterized in that: in the step (C), polymeric adsorbent be in every batch processed carry out the resin desorption and regeneration behind the waste water of 5～10 resin bed volumes, in the step (E), polymeric adsorbent be in every batch processed carry out the resin desorption and regeneration behind the waste water of 10～20 resin bed volumes.
9. according to the treatment process of the described waste water from meta dinitro benzene production of claim 3, it is characterized in that the macroporous resin in step (B) and the step (D) is ND-1507 complexing polymeric adsorbent, NDA-99 and NDA-88 complex function adsorption resin and D301 resin, also can be AmberliteIRA96, IRA93 macroporous resin that U.S. Rohm Haas company produces.
10. according to the treatment process of the waste water from meta dinitro benzene production described in the claim 4～9, it is characterized in that: step (B) and (D) described in adsorption tower can adopt the operation scheme of double-column in series absorption, single tower desorption; I, II, three adsorption towers of III are set, and with I, II tower series connection following current absorption, the I tower is as first post earlier, the II tower after the absorption of I tower is saturated, switches to II, III tower series connection following current absorption as stern post, the II tower is as first post, and the III tower is as stern post, and the I tower carries out desorption and regeneration with desorbing agent simultaneously.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102417249A (en) * | 2010-09-28 | 2012-04-18 | 中国石油化工股份有限公司 | Method for treating nitrobenzene waste water |
| CN102516082A (en) * | 2011-11-28 | 2012-06-27 | 烟台万华聚氨酯股份有限公司 | Method for preparing nitrobenzene through reacting benzene with mixed acid and washing crude nitrobenzene product |
| WO2013123780A1 (en) * | 2012-02-21 | 2013-08-29 | 南京大学 | Advanced treatment method for biochemical tail water of coking wastewater |
| CN103539285A (en) * | 2013-10-28 | 2014-01-29 | 常州大学 | Treating method for recycling wastewater of N-methylaniline production |
| CN104261503A (en) * | 2014-09-15 | 2015-01-07 | 北京理工大学 | Treatment method of nitration wastewater in TATB (triamino trinitrobenzene) production technique |
| CN109534532A (en) * | 2018-12-28 | 2019-03-29 | 浙江长征化工有限公司 | 1-CHLORO-2,4-DINITROBENZENE produces the processing method of waste water and implements the equipment of this method |
| CN110194721A (en) * | 2019-06-06 | 2019-09-03 | 浙江工业大学 | A kind of hydroxyphenylglycine centrifuge mother liquor processing unit and method |
| CN111268843A (en) * | 2020-02-28 | 2020-06-12 | 河北大鹏医药化工有限公司 | Process for recovering nitric acid from nitrified wastewater |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4804480A (en) * | 1986-12-29 | 1989-02-14 | E. I. Du Pont De Nemours And Company | Destruction of nitrophenols |
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2005
- 2005-10-21 CN CNB2005100949309A patent/CN100334016C/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102417249A (en) * | 2010-09-28 | 2012-04-18 | 中国石油化工股份有限公司 | Method for treating nitrobenzene waste water |
| CN102516082A (en) * | 2011-11-28 | 2012-06-27 | 烟台万华聚氨酯股份有限公司 | Method for preparing nitrobenzene through reacting benzene with mixed acid and washing crude nitrobenzene product |
| WO2013123780A1 (en) * | 2012-02-21 | 2013-08-29 | 南京大学 | Advanced treatment method for biochemical tail water of coking wastewater |
| US9573825B2 (en) | 2012-02-21 | 2017-02-21 | Nanjing University | Advanced treatment method for biochemical tail water of coking wastewater |
| CN103539285A (en) * | 2013-10-28 | 2014-01-29 | 常州大学 | Treating method for recycling wastewater of N-methylaniline production |
| CN103539285B (en) * | 2013-10-28 | 2015-08-26 | 常州大学 | The treatment process that a kind of wastewater of N-methylaniline production recycles |
| CN104261503A (en) * | 2014-09-15 | 2015-01-07 | 北京理工大学 | Treatment method of nitration wastewater in TATB (triamino trinitrobenzene) production technique |
| CN109534532A (en) * | 2018-12-28 | 2019-03-29 | 浙江长征化工有限公司 | 1-CHLORO-2,4-DINITROBENZENE produces the processing method of waste water and implements the equipment of this method |
| CN110194721A (en) * | 2019-06-06 | 2019-09-03 | 浙江工业大学 | A kind of hydroxyphenylglycine centrifuge mother liquor processing unit and method |
| CN110194721B (en) * | 2019-06-06 | 2022-05-24 | 浙江工业大学 | Hydroxyphenylglycine centrifugal mother liquor treatment device and method |
| CN111268843A (en) * | 2020-02-28 | 2020-06-12 | 河北大鹏医药化工有限公司 | Process for recovering nitric acid from nitrified wastewater |
| CN111268843B (en) * | 2020-02-28 | 2022-04-22 | 河北大鹏医药化工有限公司 | Process for recovering nitric acid from nitrified wastewater |
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