CN104003565A - Method for recycling liquid waste containing multiple components in production of high performance aramid fiber - Google Patents
Method for recycling liquid waste containing multiple components in production of high performance aramid fiber Download PDFInfo
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- CN104003565A CN104003565A CN201410230638.4A CN201410230638A CN104003565A CN 104003565 A CN104003565 A CN 104003565A CN 201410230638 A CN201410230638 A CN 201410230638A CN 104003565 A CN104003565 A CN 104003565A
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- extraction agent
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- aramid fiber
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- 238000000034 method Methods 0.000 title claims abstract description 46
- 229920006231 aramid fiber Polymers 0.000 title claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 238000004064 recycling Methods 0.000 title abstract description 6
- 239000010808 liquid waste Substances 0.000 title abstract 3
- 239000007788 liquid Substances 0.000 claims abstract description 48
- 238000007380 fibre production Methods 0.000 claims abstract description 23
- 238000004821 distillation Methods 0.000 claims abstract description 6
- 238000000605 extraction Methods 0.000 claims description 58
- 239000002699 waste material Substances 0.000 claims description 56
- 239000003795 chemical substances by application Substances 0.000 claims description 54
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims description 21
- 238000011084 recovery Methods 0.000 claims description 14
- 239000002351 wastewater Substances 0.000 claims description 14
- 239000002904 solvent Substances 0.000 claims description 12
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 claims description 11
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 claims description 10
- 150000001408 amides Chemical class 0.000 claims description 10
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 9
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 9
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 239000001110 calcium chloride Substances 0.000 claims description 9
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 9
- 238000006386 neutralization reaction Methods 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 7
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 6
- 230000003472 neutralizing effect Effects 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 239000011259 mixed solution Substances 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 239000006200 vaporizer Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 3
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 3
- -1 poly(isophthaloyl metaphenylene diamine Chemical compound 0.000 description 5
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000000835 fiber Substances 0.000 description 3
- MHABMANUFPZXEB-UHFFFAOYSA-N O-demethyl-aloesaponarin I Natural products O=C1C2=CC=CC(O)=C2C(=O)C2=C1C=C(O)C(C(O)=O)=C2C MHABMANUFPZXEB-UHFFFAOYSA-N 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 235000010627 Phaseolus vulgaris Nutrition 0.000 description 1
- 244000046052 Phaseolus vulgaris Species 0.000 description 1
- 239000004760 aramid Substances 0.000 description 1
- 229920003235 aromatic polyamide Polymers 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for recycling liquid waste containing multiple components in production of high performance aramid fiber. The method adopts the steps of extracting and distilling sequentially, the liquids from the top of a first tower are simultaneously concentrated by an evaporator, so that the requirements of fiber production and recycling of the liquid waste are met, the problem of high energy consumption of common distillation is solved, the economical purpose of recycling is achieved, the economic benefits are improved, the production cost is lowered, the environment is not polluted and the energy is saved.
Description
Technical field
The present invention relates to the recovery method of many components waste liquid in a kind of high-performance aramid fiber production process, be specifically related to the recovery method of the many components waste liquid in a kind of high-performance poly mpd-i fiber production process.
Background technology
In prior art, poly(isophthaloyl metaphenylene diamine) polymkeric substance is processed through neutralization, filtration and deaeration, by shower nozzle coagulation forming inside solidification liquid, again by drawing-off, washing, oven dry and sizing, the high-performance polyisophthaloyl metaphenylene diamide fibre finally obtaining, the intensity of high-performance polyisophthaloyl metaphenylene diamide fibre is very high, and its cross section is not regular circular or oval, but irregular broadband shape or waist beans shape.In the production process of high-performance polyisophthaloyl metaphenylene diamide fibre, can produce waste liquid, the moiety of waste liquid has: amide solvent, salt and dispersion agent etc., the component of the waste water that polyisophthaloyl metaphenylene diamide fibre production process produces is various, the component more complicated of waste water, to the recycling of its waste water and at present domestic and international rare its technology of introducing of recycle utilization.With general distillation technology, be difficult to each component separation totally, the needed energy consumption of sepn process is very high, and power consumption is serious, and very high to the processing cost of waste liquid, economic benefit is very low.Therefore, be necessary to improve.
Summary of the invention
The deficiency existing for prior art; the recovery method that the object of this invention is to provide many components waste liquid in a kind of high-performance aramid fiber production process, it reaches the object that can recycle, reduce production costs, protect production environment more to save the method for energy consumption.
To achieve these goals, the technical solution adopted in the present invention is.
A recovery method for many components waste liquid in high-performance aramid fiber production process, comprises the following steps:
Waste collection step, arrives waste liquor storage tank the many components waste collection in high-performance poly mpd-i fiber production process;
Neutralization procedure, in by pump, the waste liquid in waste liquor storage tank being passed to and basin, waste liquid and in and the neutralization of the neutralizing agent in basin, the pH value of waste liquid is transferred to 6.8～7.2;
Compression filtration step, in and waste liquid in basin through Filter Press, suspended substance filtration wherein totally, by pump delivery, arrive middle vessel;
Extraction step, waste liquid in middle vessel enters the bottom of the first tower by pump delivery, from the top of the first tower, according to the ratio of setting, carry extraction agent simultaneously, the filler with high mixed effect is filled in the first tower the inside, waste liquid and extraction agent mix fully in the first tower the inside, from extraction phase out at the bottom of tower, leave in the 4th basin
Concentration step, from the tower top of the first tower liquid out, is transported to vaporizer and carries out concentration, and what output reached that fiber production recycles requires the first finished product containing the calcium chloride of a small amount of glycerol;
Extraction agent is deviate from step, the mixed solution of the 4th basin enters the top of the second tower by pump delivery, in the second tower, carry out the processing of deviating from of extraction agent, from the top output of the second tower, reach the second finished product extraction agent that recycles requirement, extraction agent enters the 5th basin after by condenser condenses, the extraction agent of the 5th basin is the top to the first tower by pump delivery, recycles extraction agent;
Dehydrating step, the still bed material of the second tower, by the top of pump delivery to the three towers, carries out processed;
Rectification step, the kettle base solution of the 3rd tower, by the top of pump delivery to the four towers, carries out rectification process;
Finished product, amide solvent pure, polymerization-grade is from the top output of the 4th tower, amide solvent is by after the condenser condenses of tower top, and collection obtains the amide solvent finished product that can again put into production and recycle, and at the bottom of the still of the 4th tower, heavy component arrives waste water basin or burning disposal by pump delivery.
Further, in technical scheme, in described waste collection step, waste liquid includes 10～40% N,N-DIMETHYLACETAMIDEs, 5～20% calcium chloride or magnesium chloride, 0～10% glycerol or ethylene glycol, surplus is water.
Further, in technical scheme, in described neutralization procedure, neutralizing agent is selected calcium hydroxide or sodium hydroxide.
Further, in technical scheme, in described extraction step, extraction agent is selected chloroform, and from the top of the first tower, carrying the ratio of extraction agent is extraction agent: N,N-DIMETHYLACETAMIDE effective content=5～10:1 waste water.
Further, in technical scheme, in described extraction step, extraction agent is selected chloroform, and from the top of the first tower, carrying the ratio of extraction agent is extraction agent: N,N-DIMETHYLACETAMIDE effective content=6～8:1 waste water.
Further, in technical scheme, described extraction agent is deviate from step, and the second tower is selected the atmospheric distillation tower of mono-disperse, and the temperature of tower reactor is controlled at 105～120 degree, and the temperature of tower top is controlled at 60～80 degree by backflow.
Further, in technical scheme, described the 3rd tower is selected the vacuum still of mono-disperse, and the temperature of tower reactor is controlled at 115～130 degree, and the temperature of tower top is controlled at 60～80 degree, and vacuum degree control is at-0.07Mpa～-0.09Mpa.
Further, in technical scheme, described the 4th tower is selected the vacuum still of mono-disperse, and the temperature of tower reactor is controlled at 120～130 degree, and the temperature of tower top is controlled at 110～120 degree, and vacuum degree control is at-0.07Mpa～-0.09Mpa.
Adopt after said structure, the advantage that compared to the prior art the present invention had is: the present invention adopts and first extracts the way of distilling afterwards, by vaporizer, the tower top of the first tower liquid is out carried out to concentration simultaneously, can reach the requirement that fiber production recycles, solve common distillation and processed the high problem of energy consumption, reach the economic aim recycling, increase economic efficiency, reduce production costs, do not pollute the environment simultaneously, environmental protection and energy saving.
Accompanying drawing explanation
Below in conjunction with drawings and Examples, the present invention is further described.
Fig. 1 is schematic flow sheet of the present invention.
Embodiment
The following stated is only preferred embodiment of the present invention, does not therefore limit protection scope of the present invention.
Embodiment
A recovery method for many components waste liquid in high-performance aramid fiber production process, comprises the following steps:
Waste collection step, the many components waste collection in high-performance poly mpd-i fiber production process, to waste liquor storage tank, waste liquid includes 10～40% N,N-DIMETHYLACETAMIDEs, 5～20% calcium chloride or magnesium chloride, 0～10% glycerol or ethylene glycol, surplus is water;
Neutralization procedure, in by pump, the waste liquid in waste liquor storage tank being passed to and basin, waste liquid and in and the neutralization of the neutralizing agent in basin, neutralizing agent is selected calcium hydroxide or sodium hydroxide, the pH value of waste liquid is transferred to 6.8～7.2;
Compression filtration step, in and waste liquid in basin through Filter Press, suspended substance filtration wherein totally, by pump delivery, arrive middle vessel;
Extraction step, the waste liquid in middle vessel enters the bottom of the first tower by pump delivery, carry extraction agent from the top of the first tower according to the ratio of setting simultaneously; Extraction agent is selected chloroform, from the top of the first tower, carrying the ratio of extraction agent is extraction agent: N,N-DIMETHYLACETAMIDE effective content=5～10:1 waste water, wherein, carrying the preferred proportion scope of extraction agent is extraction agent: N,N-DIMETHYLACETAMIDE effective content=6～8:1 in waste water.The filler with high mixed effect is filled in the first tower the inside, and waste liquid and extraction agent mix fully in the first tower the inside, from extraction phase out at the bottom of tower, leaves in the 4th basin;
Concentration step, from the tower top of the first tower liquid out, is transported to vaporizer and carries out concentration, and what output reached that fiber production recycles requires the first finished product containing the calcium chloride of a small amount of glycerol;
Extraction agent is deviate from step, and the second tower is selected the atmospheric distillation tower of mono-disperse, and the temperature of tower reactor is controlled at 105～120 degree, and the temperature of tower top is controlled at 60～80 degree by backflow; The mixed solution of the 4th basin enters the top of the second tower by pump delivery, in the second tower, carry out the processing of deviating from of extraction agent, from the top output of the second tower, reach the second finished product extraction agent that recycles requirement, extraction agent enters the 5th basin after by condenser condenses, the extraction agent of the 5th basin is the top to the first tower by pump delivery, recycles extraction agent;
Dehydrating step, the 3rd tower is selected the vacuum still of mono-disperse, and the temperature of tower reactor is controlled at 115～130 degree, and the temperature of tower top is controlled at 60～80 degree, and vacuum degree control is at-0.07Mpa～-0.09Mpa; The still bed material of the second tower, by the top of pump delivery to the three towers, carries out processed;
Rectification step, the 4th tower is selected the vacuum still of mono-disperse, and the temperature of tower reactor is controlled at 120～130 degree, and the temperature of tower top is controlled at 110～120 degree, and vacuum degree control is at-0.07Mpa～-0.09Mpa; The kettle base solution of the 3rd tower, by the top of pump delivery to the four towers, carries out rectification process;
Finished product, amide solvent pure, polymerization-grade is from the top output of the 4th tower, amide solvent is by after the condenser condenses of tower top, and collection obtains the amide solvent finished product that can again put into production and recycle, and at the bottom of the still of the 4th tower, heavy component arrives waste water basin or burning disposal by pump delivery.
Below in conjunction with experimental data, further illustrate the present invention.
After waste liquid is processed by the first tower, its experimental data is as shown in table 1～3.
Waste liquid component is: containing N,N-DIMETHYLACETAMIDE 7% and calcium chloride 10%, experimental data is as shown in table 1.
Table 1
Waste liquid component is: containing N,N-DIMETHYLACETAMIDE 10%, calcium chloride 12% and glycerol 2%, experimental data is as shown in table 2.
Table 2
Waste liquid component is: containing N,N-DIMETHYLACETAMIDE 20% and calcium chloride 22%, experimental data is as shown in table 2.
Table 3
From above-mentioned data, can find out, ratio increase along with extraction agent, the direction that the data of extracting phase are become better, but too high ratio is also worthless, because too high ratio regular meeting causes the amount of de-extraction agent below to increase, energy consumption also just increases to some extent, conventionally extraction agent: N,N-DIMETHYLACETAMIDE effective content=5～10:1 in waste water; More preferably extraction agent: N,N-DIMETHYLACETAMIDE effective content=6～8:1 in waste water.
The present invention, for the separating treatment of mixed solution, processes the first tower extraction tower reactor mixed solution out respectively by the second tower, the 3rd tower and the 4th tower, its experimental data is as shown in table 4～6.
| The second tower | Inlet amount | Tower reactor discharging | Discharging data | Tower top temperature | Tower reactor temperature | Reflux |
| 1 | 2500kg/h | 600kg/h | DMAC:88.65％, | 68 | 117 | 200kg/h |
| 2 | 4500kg/h | 1000kg/h | DMAC:85.26％, | 70 | 122 | 400kg/h |
Table 4
| The 3rd tower | Tower reactor discharging | Discharging data | Tower top temperature | Tower reactor temperature | Reflux | Tower vacuum |
| 1 | 520kg/h | Moisture content 150ppm | 74 | 120 | 50 | -0.082mpa |
| 2 | 830kg/h | Moisture content 260ppm | 86 | 127 | 80 | -0.085mpa |
Table 5
Table 6
From the data of the 4th tower, can find out, the product water white transparency that the present invention obtains, and moisture is extremely low, the top standard of the quality product of solvent in colleague.Due in meta-aramid synthetic, the impact of moisture is very large, so the Disposal quality of solvent quality is closely related with the quality product of aramid fiber.
Above content is only preferred embodiment of the present invention, for those of ordinary skill in the art, according to thought of the present invention, all will change in specific embodiments and applications, and this description should not be construed as limitation of the present invention.
Claims (8)
1. a recovery method for many components waste liquid in high-performance aramid fiber production process, is characterized in that, comprises the following steps:
Waste collection step, arrives waste liquor storage tank the many components waste collection in high-performance poly mpd-i fiber production process;
Neutralization procedure, in by pump, the waste liquid in waste liquor storage tank being passed to and basin, waste liquid and in and the neutralization of the neutralizing agent in basin, the pH value of waste liquid is transferred to 6.8～7.2;
Compression filtration step, in and waste liquid in basin through Filter Press, suspended substance filtration wherein totally, by pump delivery, arrive middle vessel;
Extraction step, waste liquid in middle vessel enters the bottom of the first tower by pump delivery, from the top of the first tower, according to the ratio of setting, carry extraction agent simultaneously, the filler with high mixed effect is filled in the first tower the inside, waste liquid and extraction agent mix fully in the first tower the inside, from extraction phase out at the bottom of tower, leave in the 4th basin
Concentration step, from the tower top of the first tower liquid out, is transported to vaporizer and carries out concentration, and what output reached that fiber production recycles requires the first finished product containing the calcium chloride of a small amount of glycerol;
Extraction agent is deviate from step, the mixed solution of the 4th basin enters the top of the second tower by pump delivery, in the second tower, carry out the processing of deviating from of extraction agent, from the top output of the second tower, reach the second finished product extraction agent that recycles requirement, extraction agent enters the 5th basin after by condenser condenses, the extraction agent of the 5th basin is the top to the first tower by pump delivery, recycles extraction agent;
Dehydrating step, the still bed material of the second tower, by the top of pump delivery to the three towers, carries out processed;
Rectification step, the kettle base solution of the 3rd tower, by the top of pump delivery to the four towers, carries out rectification process;
Finished product, amide solvent pure, polymerization-grade is from the top output of the 4th tower, amide solvent is by after the condenser condenses of tower top, and collection obtains the amide solvent finished product that can again put into production and recycle, and at the bottom of the still of the 4th tower, heavy component arrives waste water basin or burning disposal by pump delivery.
2. the recovery method of many components waste liquid in a kind of high-performance aramid fiber production process according to claim 1, it is characterized in that: in described waste collection step, waste liquid includes 10～40% N,N-DIMETHYLACETAMIDEs, 5～20% calcium chloride or magnesium chloride, 0～10% glycerol or ethylene glycol, surplus is water.
3. the recovery method of many components waste liquid in a kind of high-performance aramid fiber production process according to claim 1, is characterized in that: in described neutralization procedure, neutralizing agent is selected calcium hydroxide or sodium hydroxide.
4. the recovery method of many components waste liquid in a kind of high-performance aramid fiber production process according to claim 1, it is characterized in that: in described extraction step, extraction agent is selected chloroform, and from the top of the first tower, carrying the ratio of extraction agent is extraction agent: N,N-DIMETHYLACETAMIDE effective content=5～10:1 waste water.
5. the recovery method of many components waste liquid in a kind of high-performance aramid fiber production process according to claim 1, it is characterized in that: in described extraction step, extraction agent is selected chloroform, and from the top of the first tower, carrying the ratio of extraction agent is extraction agent: N,N-DIMETHYLACETAMIDE effective content=6～8:1 waste water.
6. the recovery method of many components waste liquid in a kind of high-performance aramid fiber production process according to claim 1, it is characterized in that: described extraction agent is deviate from step, the second tower is selected the atmospheric distillation tower of mono-disperse, the temperature of tower reactor is controlled at 105～120 degree, and the temperature of tower top is controlled at 60～80 degree by backflow.
7. the recovery method of many components waste liquid in a kind of high-performance aramid fiber production process according to claim 1, it is characterized in that: described the 3rd tower is selected the vacuum still of mono-disperse, the temperature of tower reactor is controlled at 115～130 degree, the temperature of tower top is controlled at 60～80 degree, and vacuum degree control is at-0.07Mpa～-0.09Mpa.
8. the recovery method of many components waste liquid in a kind of high-performance aramid fiber production process according to claim 1, it is characterized in that: described the 4th tower is selected the vacuum still of mono-disperse, the temperature of tower reactor is controlled at 120～130 degree, the temperature of tower top is controlled at 110～120 degree, and vacuum degree control is at-0.07Mpa～-0.09Mpa.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105645501A (en) * | 2015-12-14 | 2016-06-08 | 长春工业大学 | Method for recovering N,N-dimethyl acetamide from pharmaceutical wastewater |
| CN105646271A (en) * | 2015-12-08 | 2016-06-08 | 长春工业大学 | Method for recovering N,N-dimethyl acetamide from waste liquid generated in cefuroxime acid production through extraction |
| CN109134339A (en) * | 2018-09-13 | 2019-01-04 | 清华大学 | Method for recovering solvents is used in a kind of production of para-aramid fiber |
| CN111807593A (en) * | 2020-07-23 | 2020-10-23 | 河南神马尼龙化工有限责任公司 | Integrated device and process for treating and utilizing salt-containing organic wastewater in para-aramid solvent workshop section |
| CN114350016A (en) * | 2021-12-24 | 2022-04-15 | 余姚大发化纤有限公司 | Method and production system for removing spandex in waste polyester textiles |
| CN114350017A (en) * | 2022-01-26 | 2022-04-15 | 余姚大发化纤有限公司 | Production system for efficiently removing spandex in waste polyester textiles |
| CN114436359A (en) * | 2020-10-19 | 2022-05-06 | 中国石油化工股份有限公司 | Method for extracting and recovering N, N-dimethylacetamide in wastewater |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101774720A (en) * | 2009-12-24 | 2010-07-14 | 烟台氨纶股份有限公司 | Treatment method of waste liquid containing butanediol and DMAC (dimethylacetamide) during production of aramid fiber fibrid |
| CN101774721A (en) * | 2009-12-24 | 2010-07-14 | 烟台氨纶股份有限公司 | Method for treating production solvent-containing waste liquid from production of m-aramid fibers |
| CN102285731A (en) * | 2011-05-31 | 2011-12-21 | 上海舟汉纤维材料科技有限公司 | Treatment method and treatment device of sulfuric acid wastewater in production process of polyphenylene terephthalamide fibers |
| CN103526321A (en) * | 2013-09-27 | 2014-01-22 | 东莞市灿森新材料有限公司 | Preparation method of high-performance polyisophthaloyl metaphenylene diamine fiber |
-
2014
- 2014-05-28 CN CN201410230638.4A patent/CN104003565B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101774720A (en) * | 2009-12-24 | 2010-07-14 | 烟台氨纶股份有限公司 | Treatment method of waste liquid containing butanediol and DMAC (dimethylacetamide) during production of aramid fiber fibrid |
| CN101774721A (en) * | 2009-12-24 | 2010-07-14 | 烟台氨纶股份有限公司 | Method for treating production solvent-containing waste liquid from production of m-aramid fibers |
| CN102285731A (en) * | 2011-05-31 | 2011-12-21 | 上海舟汉纤维材料科技有限公司 | Treatment method and treatment device of sulfuric acid wastewater in production process of polyphenylene terephthalamide fibers |
| CN103526321A (en) * | 2013-09-27 | 2014-01-22 | 东莞市灿森新材料有限公司 | Preparation method of high-performance polyisophthaloyl metaphenylene diamine fiber |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105646271A (en) * | 2015-12-08 | 2016-06-08 | 长春工业大学 | Method for recovering N,N-dimethyl acetamide from waste liquid generated in cefuroxime acid production through extraction |
| CN105645501A (en) * | 2015-12-14 | 2016-06-08 | 长春工业大学 | Method for recovering N,N-dimethyl acetamide from pharmaceutical wastewater |
| CN109134339A (en) * | 2018-09-13 | 2019-01-04 | 清华大学 | Method for recovering solvents is used in a kind of production of para-aramid fiber |
| CN111807593A (en) * | 2020-07-23 | 2020-10-23 | 河南神马尼龙化工有限责任公司 | Integrated device and process for treating and utilizing salt-containing organic wastewater in para-aramid solvent workshop section |
| CN111807593B (en) * | 2020-07-23 | 2023-07-18 | 河南神马芳纶技术开发有限公司 | Salt-containing organic wastewater treatment and utilization integrated device and process for para-aramid solvent working section |
| CN114436359A (en) * | 2020-10-19 | 2022-05-06 | 中国石油化工股份有限公司 | Method for extracting and recovering N, N-dimethylacetamide in wastewater |
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