CN104016871A - Method for recycling anthranilic acid from methyl anthranilate wastewater - Google Patents
Method for recycling anthranilic acid from methyl anthranilate wastewater Download PDFInfo
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- CN104016871A CN104016871A CN201410256017.3A CN201410256017A CN104016871A CN 104016871 A CN104016871 A CN 104016871A CN 201410256017 A CN201410256017 A CN 201410256017A CN 104016871 A CN104016871 A CN 104016871A
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C227/00—Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
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- C07C227/40—Separation; Purification
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Abstract
The invention provides a method for recycling an anthranilic acid from methyl anthranilate wastewater. The method comprises the following steps: separating and extracting the methyl anthranilate wastewater so as to obtain a methyl anthranilate sodium solution; and then purifying the methyl anthranilate sodium solution so as to obtain anthranilic acid. According to the method, anthranilic acid is purified by utilizing the characteristics of anthranilic acid which is soluble in hot water and slightly soluble in cold water, so that the processes of addition and purification of other materials are reduced. Thus, the purification cost is lowered while the economy and the environmental friendliness are realized.
Description
Technical field
The present invention relates to chemical field, be specifically related to a kind of method that reclaims anthranilic acid from methyl o-aminobenzoate waste water.
Background technology
Methyl o-aminobenzoate, chemical formula C
8h
9nO
2, be a kind of colourless crystallization or light yellow liquid, long-term exposure variable color, can volatilize with water vapour, is soluble in ethanol and ether, and its ethanolic soln, with blue-fluorescence, dissolves in most expressed oils and propylene glycol, is slightly dissolved in mineral oil, is slightly soluble in water, is insoluble to glycerine.
Methyl o-aminobenzoate can be used as the intermediate of dyestuff, medicine, agricultural chemicals, spices.Aspect dyestuff, for the manufacture of azoic dyestuff, anthraquinone dye, indigoids dyestuff.For example DISPERSE YELLOW GC, DISPERSE YELLOW 5G, DISPERSE ORANGE 30 200 GG, active brown K-B3Y, neutral blue BNL.Aspect medical, for the manufacture of Anti-arrhythmic Agent Changrolin, vitamin(e) L, nonsteroidal anti-inflammatory analgetic vialidon, benzydamine, non-barbiturates soporific turzolon, major tranquilizer tardan.Anthranilic acid, as chemical reagent, can be used for measuring the complexometric reagent of cadmium, cobalt, mercury, magnesium, nickel, lead, zinc and cerium etc., shares and can measure nitrite with naphthalidine.These product are also for other organic syntheses.
In methyl o-aminobenzoate production process, owing to relating to, raw material is many, Production Flow Chart long, side reaction is many, cause and in production process, produce a large amount of complicated components, concentration, organic waste water that colourity is high, and majority belongs to recalcitrant substance (methyl o-aminobenzoate, anthranilic acid, methyl alcohol, 0-chloro-benzoic acid methyl esters), thereby bring difficulty to wastewater treatment.The material that in methyl o-aminobenzoate waste water, content is higher is anthranilic acid.Anthranilic acid is as the intermediate of dyestuff, medicine, agricultural chemicals, spices, and tool has been widely used.
Existing methyl o-aminobenzoate waste water treatment adopts traditional materialization-biochemical combined treatment process conventionally, by intensive treatment, although also can reach emission request, but process cycle is longer, consumption pharmaceutical quantities is many, and working cost is higher, and general manufacturing enterprise is difficult to bear.Meanwhile, this treatment process is only focused on regulation effect, and ignores the recovery of useful matter, especially anthranilic acid in sewage, makes it fail rationally to be utilized, and has caused the wasting of resources.
At present, have a kind of method that adopts copper-containing waste acid water extraction anthranilic acid, the method is in waste water, to have introduced heavy metal copper ion, thereby extracts anthranilic acid.Though this method can be extracted anthranilic acid, because Xiang Shuizhong has introduced heavy metal copper ion, cause secondary pollution, be unfavorable for the aftertreatment of waste water.
Therefore, there is the treatment process that a kind of new methyl o-aminobenzoate waste water need to be provided, can from methyl o-aminobenzoate waste water, reclaim useful anthranilic acid, reach the object of resource reusing, also can make wastewater biological toxicity greatly reduce simultaneously, thereby alleviate subsequent disposal burden, methyl esters wastewater treatment process is simplified.
Summary of the invention
For solving the deficiencies in the prior art, the present invention proposes a kind of method that reclaims anthranilic acid from methyl o-aminobenzoate waste water.
Main thought of the present invention is: the o-amino benzoyl acid sodium solution that separation and extraction obtains from methyl o-aminobenzoate waste water, then obtain anthranilic acid after purified processing.
In order to achieve the above object, the invention provides a kind of method that reclaims anthranilic acid from methyl o-aminobenzoate waste water, described method is that methyl o-aminobenzoate waste water is carried out to separating treatment and extraction process, then obtain o-amino benzoyl acid sodium solution, then obtain anthranilic acid after purified processing; Wherein, described purification process be to separation and extraction obtain that o-amino benzoyl acid sodium solution decolours, acid out, pyrolysis, decolour again, separate out separate and suction filtration except water treatment, finally obtain anthranilic acid.
In an embodiment of the present invention, described purification process comprises the following steps:
(1) o-amino benzoyl acid sodium solution separation and extraction being obtained decolours;
(2) the o-amino benzoyl acid sodium solution after decolouring is carried out to acid out processing, after suction filtration dehydration, obtain anthranilic acid wet feed;
(3) at 80～95 DEG C, described anthranilic acid wet feed is carried out after thermal hydrolysis processing, then the processing of decolouring, filtrate after suction filtration, obtained;
(4) filtrate is lowered the temperature after processing, obtained precipitate, suction filtration dewaters and is dried the rear anthranilic acid that obtains.
In the present invention's one preferred embodiment, in described step (1), use gac to decolour, the proportional range of gac and o-amino benzoyl acid sodium solution is (0.5～2) kg:100 L, the decolouring treatment time is 10～20 minutes; Preferably, the ratio of described gac and o-amino benzoyl acid sodium solution is 1 kg:100 L.
In the present invention's one preferred embodiment, the pH value of the acid out processing of described step (2) is 3.5～4.0, and the time of acid out processing is 1～10 minute; Preferably, the time of described acid out processing is 5 minutes.
In the present invention's one preferred embodiment, in the thermal hydrolysis of described step (3) is processed, the proportional range of water and anthranilic acid wet feed is 10 L:(2～6) kg, preferably 10 L:4kg; In the decolouring of described step (3) is processed, use gac to decolour, the proportional range of gac and o-amino benzoyl acid sodium solution is (0.1～1) kg:100 L, preferably 0.5 kg:100 L, and the decolouring treatment time is 10～20 minutes.
In an embodiment of the present invention, the described separating treatment that methyl o-aminobenzoate waste water is carried out is that to regulate the pH value of methyl o-aminobenzoate waste water be to carry out single-stage extraction processing after 3～4, after biphase equilibrium, carry out oily water separation, the anthranilic acid in described methyl o-aminobenzoate waste water is loaded in extraction agent.
In the present invention's one preferred embodiment, the volume ratio of described methyl o-aminobenzoate waste water and extraction agent is 1:10.
In the present invention's one preferred embodiment, described extraction agent is the mixture of tributyl phosphate and aviation kerosene.
In the present invention's one preferred embodiment, the volume ratio scope of described tributyl phosphate and aviation kerosene is (1～5): (5～9), preferably 3:7.
In an embodiment of the present invention, the described extraction process that methyl o-aminobenzoate waste water is carried out is to have the extraction agent of anthranilic acid to add in NaOH solution described load to carry out the molten processing of alkali, and the water obtaining after separating is o-amino benzoyl acid sodium solution.
In the present invention's one preferred embodiment, in the molten processing of described alkali, it is (2～8) that described load has the extraction agent of anthranilic acid and the volume ratio scope of NaOH solution: 1, and preferably 5:1.
In the present invention's one preferred embodiment, a kind of method that reclaims anthranilic acid from methyl o-aminobenzoate waste water is provided, described method is that methyl o-aminobenzoate waste water is carried out to separating treatment and extraction process, then obtain o-amino benzoyl acid sodium solution, then obtain anthranilic acid after purified processing; Wherein,
Described separating treatment is that to regulate the pH value of methyl o-aminobenzoate waste water be to carry out single-stage extraction processing after 3～4, after biphase equilibrium, carry out oily water separation, anthranilic acid in described methyl o-aminobenzoate waste water is loaded in extraction agent, and the volume ratio of described methyl o-aminobenzoate waste water and extraction agent is 1:10; Described extraction agent is the mixture of tributyl phosphate and aviation kerosene, and the volume ratio of described tributyl phosphate and aviation kerosene is 3:7; Meanwhile,
Described extraction process is to have the extraction agent of anthranilic acid to add in NaOH solution the load of above-mentioned separating treatment acquisition to carry out the molten processing of alkali, and the water obtaining after separating is o-amino benzoyl acid sodium solution; Wherein, in the molten processing of described alkali, it is 5:1 that described load has the extraction agent of anthranilic acid and the volume ratio of NaOH solution;
Described purification process is that the o-amino benzoyl acid sodium solution that said extracted is obtained decolours, acid out, pyrolysis, decolour again, separate out separate and suction filtration except water treatment, finally obtain anthranilic acid, specifically comprise the following steps:
(1) the o-amino benzoyl acid sodium solution that uses gac to obtain separation and extraction decolours, and wherein, the ratio of gac and o-amino benzoyl acid sodium solution is 1 kg:100 L, and the decolouring treatment time is 10～20 minutes;
(2) the o-amino benzoyl acid sodium solution after decolouring is carried out to pH regulator, making o-amino benzoyl acid sodium solution is to carry out acid out for 3.5～4.0 times to process 5 minutes in pH value, after suction filtration dehydration, obtains anthranilic acid wet feed;
(3) at 80～95 DEG C, described anthranilic acid wet feed is carried out to thermal hydrolysis processing, re-use the gac processing of decolouring after anthranilic acid wet feed is dissolved completely, after suction filtration, obtain filtrate; Wherein, in described thermal hydrolysis is processed, the ratio of water and anthranilic acid wet feed is 10 L:4kg; In described decolouring is processed, the ratio of gac and o-amino benzoyl acid sodium solution is 0.5 kg:100 L, and the decolouring treatment time is 10～20 minutes;
(4) filtrate is lowered the temperature after processing, obtained precipitate, suction filtration dewaters and is dried the rear anthranilic acid that obtains.
Particularly preferably, in the separating treatment of above-described embodiment, can working concentration the technical hydrochloric acid that is 30% regulate the pH value of methyl o-aminobenzoate waste water; In extraction process, can functional quality mark be 15% NaOH solution has the extraction agent of anthranilic acid to carry out the molten processing of alkali to load.
It should be noted that, if no special instructions, the reagent relating in the present invention is commercial reagent.
In the present invention, utilize anthranilic acid to be dissolved in the characteristic that hot water is slightly soluble in cold water it is purified, reduced adding and purifying flow process of other material, economic environmental protection again when reducing purifying cost.
The beneficial effect that the present invention has:
(1) avoid in waste water, introducing heavy metal copper ion, avoided the generation of secondary pollution, be more conducive to the aftertreatment of waste water;
(2) o-amino benzoyl acid recovering rate of the present invention reaches more than 98%, can significantly reduce toxic organic compound content in waste water, and the waste water of therefore isolating after anthranilic acid has good biodegradable, and subsequent disposal is simplified;
(3) the present invention utilizes anthranilic acid to be dissolved in the characteristic that hot water is slightly soluble in cold water it to be purified, reduced adding and purifying flow process of other material, economic environmental protection again when reducing purifying cost.
Embodiment
Below in conjunction with embodiment, the present invention is described in detail, embodiment is intended to explain and non-limiting technical scheme of the present invention.
embodiment 1.
The present embodiment provides a kind of concrete method that reclaims anthranilic acid from methyl o-aminobenzoate waste water, described method is that methyl o-aminobenzoate waste water is carried out to separating treatment and extraction process, then obtain o-amino benzoyl acid sodium solution, then obtain anthranilic acid after purified processing; Wherein, described purification process be to separation and extraction obtain that o-amino benzoyl acid sodium solution decolours, acid out, pyrolysis, decolour again, separate out separate and suction filtration except water treatment, finally obtain anthranilic acid.
Described method specifically comprises the following steps:
(1) 300L tributyl phosphate and 700L aviation kerosene are squeezed into mixing kettle, after mixing, obtain 1000L extraction agent.10000L methyl o-aminobenzoate waste water is squeezed into extraction reactor, open reactor, in waste water, add 30% technical hydrochloric acid 80L, now waste water ph is 3.5.1000L extraction agent is added in waste water, and extractive reaction stopped after 30 minutes, left standstill after 30min, separated lower floor's water, simultaneously off-loading the extraction agent of anthranilic acid;
(2) there is the extraction agent of anthranilic acid to squeeze into abstraction reaction still load in step (1), open reactor, adding massfraction is 15% liquid caustic soda 200L, reaction 10min stops, after leaving standstill 60min, carry out oily water separation, oil reservoir is the extraction agent reclaiming, and is cycled to used in the separation of the anthranilic acid in waste water.Water layer is the solution that contains anthranilic acid sodium of extraction;
(3) o-amino benzoyl acid sodium solution step (2) being obtained is squeezed into decoloring reaction still, adds 2kg gac to decolour, and decolouring is filtered after stirring 15min, obtains filter liquor; Filtrate after decolouring is squeezed into acid out still, open and stir, slowly adding content is 30% technical hydrochloric acid 38L, and material liquid PH value reaches 3.5, continues after reaction 5min, and material liquid pH value 3.7, stops stirring.By acid out liquid suction filtration, the filter cake that suction filtration obtains packs whizzer into and further dewaters, and obtains anthranilic acid wet feed 84kg;
(4) 84kg anthranilic acid wet feed is put into dissolution kettle, add the hot water 210L of 95 DEG C, stirring reaction 8min, anthranilic acid wet feed all dissolves.In dissolution kettle, add 1kg gac to decolour, 15min is stirred in decolouring.While hot by charcoal-water mixed liquid suction filtration, obtain filter liquor, filtrate is proceeded to cooling reactor to be cooled with circulating water, be down to after 30 DEG C when filtrate temperature, carry out suction filtration, filter cake packs drying in whizzer into and removes unnecessary moisture, obtain the anthranilic acid wet feed after refining, after this wet feed is dry, obtain anthranilic acid 54kg, content 97.5%.
Measure methyl esters waste water o-amino benzoyl acid content, 5780mg/L before separating, 85mg/L after separating, the rate of recovery 98.5%.
embodiment 2
The present embodiment provides a kind of concrete method that reclaims anthranilic acid from methyl o-aminobenzoate waste water, described method is that methyl o-aminobenzoate waste water is carried out to separating treatment and extraction process, then obtain o-amino benzoyl acid sodium solution, then obtain anthranilic acid after purified processing; Wherein, described purification process be to separation and extraction obtain that o-amino benzoyl acid sodium solution decolours, acid out, pyrolysis, decolour again, separate out separate and suction filtration except water treatment, finally obtain anthranilic acid.
Described method specifically comprises the following steps:
(1) 300L tributyl phosphate and 700L aviation kerosene are squeezed into mixing kettle, after mixing, obtain 1000L extraction agent.10000L methyl o-aminobenzoate waste water is squeezed into extraction reactor, open reactor, in waste water, add 30% technical hydrochloric acid 82L, now waste water PH is 3.0.1000L extraction agent is added in waste water, and extractive reaction stopped after 30 minutes, left standstill after 30min, separated lower floor's water, simultaneously off-loading the extraction agent of anthranilic acid;
(2) there is the extraction agent of anthranilic acid to squeeze into abstraction reaction still load in step (1), open reactor, adding massfraction is 15% liquid caustic soda 200L, reaction 10min stops, after leaving standstill 60min, carry out oily water separation, oil reservoir is the extraction agent reclaiming, and is cycled to used in the separation of the anthranilic acid in waste water; Water layer is the solution that contains anthranilic acid sodium of extraction;
(3) o-amino benzoyl acid sodium solution step (2) being obtained is squeezed into decoloring reaction still, adds 2kg gac to decolour, and decolouring is filtered after stirring 20min, obtains filter liquor; Filtrate after decolouring is squeezed into acid out still, open and stir, slowly adding content is 30% technical hydrochloric acid 38L, and material liquid PH value reaches 3.8, continues after reaction 5min, and material liquid pH value 4.1, continues to add hydrochloric acid 2L, and after reaction 5min, material liquid pH value 3.6, stops stirring.By acid out liquid suction filtration, the filter cake that suction filtration obtains packs whizzer into and further dewaters, and obtains anthranilic acid wet feed 91kg;
(4) 91kg anthranilic acid wet feed is put into dissolution kettle, add the hot water 228L of 80 DEG C, stirring reaction 15min, anthranilic acid wet feed all dissolves.In dissolution kettle, add 1.2kg gac to decolour, 20min is stirred in decolouring.While hot by charcoal-water mixed liquid suction filtration, obtain filter liquor, filtrate is proceeded to cooling reactor to be cooled with circulating water, be down to after 30 DEG C when filtrate temperature, carry out suction filtration, filter cake packs drying in whizzer into and removes unnecessary moisture, obtain the anthranilic acid wet feed after refining, after this wet feed is dry, obtain anthranilic acid 58.5kg, content 97.3%.
Measure methyl esters waste water o-amino benzoyl acid content, 6145mg/L before separating, 96mg/L after separating, the rate of recovery 98.4%.
embodiment 3
The present embodiment provides a kind of concrete method that reclaims anthranilic acid from methyl o-aminobenzoate waste water, described method is that methyl o-aminobenzoate waste water is carried out to separating treatment and extraction process, then obtain o-amino benzoyl acid sodium solution, then obtain anthranilic acid after purified processing; Wherein, described purification process be to separation and extraction obtain that o-amino benzoyl acid sodium solution decolours, acid out, pyrolysis, decolour again, separate out separate and suction filtration except water treatment, finally obtain anthranilic acid.
Described method specifically comprises the following steps:
(1) 10000L methyl o-aminobenzoate waste water is squeezed into extraction reactor, open reactor, in waste water, add 30% technical hydrochloric acid 79L, now waste water PH is 4.0.The extraction agent that 1000L is reclaimed adds in waste water, and extractive reaction stopped after 30 minutes, leaves standstill after 30min, separates lower floor's water, simultaneously off-loading the extraction agent of anthranilic acid;
(2) there is the extraction agent of anthranilic acid to squeeze into abstraction reaction still load in step (1), open reactor, adding massfraction is 15% liquid caustic soda 200L, reaction 10min stops, after leaving standstill 60min, carry out oily water separation, oil reservoir is the extraction agent reclaiming, and is cycled to used in the separation of the anthranilic acid in waste water.Water layer is the solution that contains anthranilic acid sodium of extraction;
(3) o-amino benzoyl acid sodium solution step (2) being obtained is squeezed into decoloring reaction still, adds 2kg gac to decolour, and decolouring is filtered after stirring 10min, obtains filter liquor; Filtrate after decolouring is squeezed into acid out still, open and stir, slowly adding content is 30% technical hydrochloric acid 38L, and material liquid PH value reaches 3.5, continues after reaction 5min, and material liquid pH value 3.6, stops stirring.By acid out liquid suction filtration, the filter cake that suction filtration obtains packs whizzer into and further dewaters, and obtains anthranilic acid wet feed 83kg;
(4) 83kg anthranilic acid wet feed is put into dissolution kettle, add the hot water 208L of 85 DEG C, stirring reaction 10min, anthranilic acid wet feed all dissolves.In dissolution kettle, add 1.1kg gac to decolour, 10min is stirred in decolouring.While hot by charcoal-water mixed liquid suction filtration, obtain filter liquor, filtrate is proceeded to cooling reactor to be cooled with circulating water, be down to after 30 DEG C when filtrate temperature, carry out suction filtration, filter cake packs drying in whizzer into and removes unnecessary moisture, obtain the anthranilic acid wet feed after refining, after this wet feed is dry, obtain anthranilic acid 56kg, content 97.8%.
Methyl esters waste water o-amino benzoyl acid content, 5748mg/L before separating, 78mg/L after separating, the rate of recovery 98.6%.
In the present invention, utilize anthranilic acid to be dissolved in the characteristic that hot water is slightly soluble in cold water it is purified, reduced adding and purifying flow process of other material, economic environmental protection again when reducing purifying cost.Simultaneously, in the method that reclaims anthranilic acid from methyl o-aminobenzoate waste water of the present invention, aminobenzoic acid recovering rate reaches more than 98%, avoid introducing heavy metal copper ion in waste water, prevent the generation of secondary pollution, can significantly reduce toxic organic compound content in waste water, the waste water that makes to isolate after anthranilic acid has good biodegradable, is more conducive to the aftertreatment of waste water simultaneously.
The present invention is described by above-mentioned related embodiment, but above-described embodiment is only for implementing example of the present invention.Must be pointed out that, published embodiment does not limit the scope of the invention.On the contrary, be contained in the spirit of claims and the amendment of scope and impartial setting is included in scope of the present invention.
Claims (10)
1. one kind is reclaimed the method for anthranilic acid from methyl o-aminobenzoate waste water, described method is that methyl o-aminobenzoate waste water is carried out to separating treatment and extraction process, then obtain o-amino benzoyl acid sodium solution, then obtain anthranilic acid after purified processing; Wherein,
Described purification process be to separation and extraction obtain that o-amino benzoyl acid sodium solution decolours, acid out, pyrolysis, decolour again, separate out separate and suction filtration except water treatment, finally obtain anthranilic acid.
2. the method for claim 1, is characterized in that, described purification process comprises the following steps:
(1) o-amino benzoyl acid sodium solution separation and extraction being obtained decolours;
(2) the o-amino benzoyl acid sodium solution after decolouring is carried out to acid out processing, after suction filtration dehydration, obtain anthranilic acid wet feed;
(3) at 80～95 DEG C, described anthranilic acid wet feed is carried out after thermal hydrolysis processing, then the processing of decolouring, filtrate after suction filtration, obtained;
(4) filtrate is lowered the temperature after processing, obtained precipitate, suction filtration dewaters and is dried the rear anthranilic acid that obtains.
3. method as claimed in claim 2, is characterized in that, uses gac to decolour in described step (1), and the ratio of gac and o-amino benzoyl acid sodium solution is (0.5～2) kg:100 L, is preferably 1 kg:100 L; The decolouring treatment time is 10～20 minutes.
4. method as claimed in claim 2, is characterized in that, the pH value of the acid out processing of described step (2) is 3.5～4.0, and the time of described acid out processing is 1～10 minute, is preferably 5 minutes.
5. method as claimed in claim 2, is characterized in that, in the thermal hydrolysis of described step (3) is processed, the ratio of water and anthranilic acid wet feed is 10 L:(2～6) kg, be preferably 10 L:4kg; In the decolouring of described step (3) is processed, use gac to decolour, the ratio of gac and o-amino benzoyl acid sodium solution is (0.1～1) kg:100 L, is preferably 0.5 kg:100 L, and the decolouring treatment time is 10～20 minutes.
6. method as claimed in claim 2, it is characterized in that, the described separating treatment that methyl o-aminobenzoate waste water is carried out is that to regulate the pH value of methyl o-aminobenzoate waste water be to carry out single-stage extraction processing after 3～4, after biphase equilibrium, carry out oily water separation, the anthranilic acid in described methyl o-aminobenzoate waste water is loaded in extraction agent.
7. method as claimed in claim 6, is characterized in that, the volume ratio of described methyl o-aminobenzoate waste water and extraction agent is 1:10.
8. method as claimed in claim 7, is characterized in that, described extraction agent is the mixture of tributyl phosphate and aviation kerosene, and the volume ratio of described tributyl phosphate and aviation kerosene is (1～5): (5～9), are preferably 3:7.
9. method as claimed in claim 2, it is characterized in that, the described extraction process that methyl o-aminobenzoate waste water is carried out is to have the extraction agent of anthranilic acid to add in NaOH solution described load to carry out the molten processing of alkali, and the water obtaining after separating is o-amino benzoyl acid sodium solution.
10. method as claimed in claim 9, is characterized in that, in the molten processing of described alkali, it is (2～8) that described load has the extraction agent of anthranilic acid and the volume ratio of NaOH solution: 1, be preferably 5:1.
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| CN104478028A (en) * | 2014-12-11 | 2015-04-01 | 沈阳化工研究院有限公司 | Treatment method of saccharin production wastewater |
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| CN111072120A (en) * | 2018-10-19 | 2020-04-28 | 上海申英环保科技有限公司 | O-aminobenzene and m-aminobenzene wastewater treatment agent and wastewater treatment method |
| CN114195665A (en) * | 2021-12-14 | 2022-03-18 | 武汉世吉药业有限公司 | Neutralization and acidification process and equipment for high-purity NCAA |
| WO2023117756A1 (en) | 2021-12-20 | 2023-06-29 | Covestro Deutschland Ag | Process for recovering aminobenzoic acid from an aqueous mother liquor |
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