CN103772230A - Method for separating mixing solution of sodium salt, dimethyl formamide, methylbenzene and water through integration of azeotropic/extractive distillation and liquid-liquid stratification - Google Patents
Method for separating mixing solution of sodium salt, dimethyl formamide, methylbenzene and water through integration of azeotropic/extractive distillation and liquid-liquid stratification Download PDFInfo
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- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 title claims abstract description 182
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 title claims abstract description 95
- 238000000034 method Methods 0.000 title claims abstract description 53
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 239000007788 liquid Substances 0.000 title claims abstract description 35
- 159000000000 sodium salts Chemical class 0.000 title claims abstract description 21
- 238000000895 extractive distillation Methods 0.000 title claims abstract description 4
- 230000010354 integration Effects 0.000 title claims description 9
- 238000002156 mixing Methods 0.000 title description 12
- 238000010533 azeotropic distillation Methods 0.000 title description 5
- 238000013517 stratification Methods 0.000 title 1
- 238000000605 extraction Methods 0.000 claims abstract description 83
- 239000011259 mixed solution Substances 0.000 claims abstract description 28
- 239000002904 solvent Substances 0.000 claims abstract description 22
- 239000000203 mixture Substances 0.000 claims abstract description 16
- 238000010612 desalination reaction Methods 0.000 claims abstract description 13
- 239000002994 raw material Substances 0.000 claims abstract description 13
- MQIUGAXCHLFZKX-UHFFFAOYSA-N Di-n-octyl phthalate Natural products CCCCCCCCOC(=O)C1=CC=CC=C1C(=O)OCCCCCCCC MQIUGAXCHLFZKX-UHFFFAOYSA-N 0.000 claims abstract description 11
- BJQHLKABXJIVAM-UHFFFAOYSA-N bis(2-ethylhexyl) phthalate Chemical compound CCCCC(CC)COC(=O)C1=CC=CC=C1C(=O)OCC(CC)CCCC BJQHLKABXJIVAM-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 238000009833 condensation Methods 0.000 claims abstract description 9
- 230000005494 condensation Effects 0.000 claims abstract description 9
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims abstract description 7
- 230000008929 regeneration Effects 0.000 claims abstract description 6
- 238000011069 regeneration method Methods 0.000 claims abstract description 6
- 238000001704 evaporation Methods 0.000 claims abstract description 5
- 230000008020 evaporation Effects 0.000 claims abstract 2
- 239000000243 solution Substances 0.000 claims description 10
- 238000004821 distillation Methods 0.000 claims description 3
- 239000012046 mixed solvent Substances 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 abstract description 17
- 238000009835 boiling Methods 0.000 abstract description 2
- 238000012986 modification Methods 0.000 description 16
- 230000004048 modification Effects 0.000 description 16
- 239000002351 wastewater Substances 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical class C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- 230000003851 biochemical process Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 238000011282 treatment Methods 0.000 description 3
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000007073 chemical hydrolysis Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 239000000575 pesticide Substances 0.000 description 2
- OCJBOOLMMGQPQU-UHFFFAOYSA-N 1,4-dichlorobenzene Chemical compound ClC1=CC=C(Cl)C=C1 OCJBOOLMMGQPQU-UHFFFAOYSA-N 0.000 description 1
- LAVCITRXCNYMBB-UHFFFAOYSA-N O.CC1=CC=CC=C1.C(=O)N(C)C.[Na] Chemical compound O.CC1=CC=CC=C1.C(=O)N(C)C.[Na] LAVCITRXCNYMBB-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229940117389 dichlorobenzene Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000004434 industrial solvent Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000011221 initial treatment Methods 0.000 description 1
- 238000000622 liquid--liquid extraction Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- QWVGKYWNOKOFNN-UHFFFAOYSA-N o-cresol Chemical compound CC1=CC=CC=C1O QWVGKYWNOKOFNN-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 125000003944 tolyl group Chemical group 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
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- Extraction Or Liquid Replacement (AREA)
Abstract
一种共沸萃取精馏与液液分层集成分离钠盐、DMF、甲苯和水混合溶液的方法，采用脱盐罐进行预热和脱盐，将共沸精馏与萃取精馏有效集成，在共沸萃取精馏塔中实现多组分分离。原料预热后由脱盐蒸发罐脱盐，脱盐后和环丁砜和邻苯二甲酸二辛酯组成的改性萃取剂加入共沸萃取精馏塔中，控制塔顶、塔底温度进行共沸萃取精馏,塔顶得到甲苯和水混合汽体，塔底得到DMF和改性萃取剂的混合物；甲苯和水混合汽体经冷凝后，分为含量99%以上甲苯层和甲苯含量低于0.08%水层；DMF和改性萃取剂的混合物经溶剂再生循环塔精馏处理，塔顶得到99.9%以上的DMF，溶剂再生循环塔塔底得到改性萃取剂，循环至共沸萃取精馏塔。
A method of azeotropic extractive rectification and liquid-liquid layering integrated separation of sodium salt, DMF, toluene and water mixed solution, using desalination tank for preheating and desalination, effectively integrating azeotropic rectification and extractive rectification, in a co- Multi-component separation is achieved in the boiling extractive distillation column. After the raw material is preheated, it is desalted by the desalination evaporation tank. After desalination, the modified extraction agent composed of sulfolane and dioctyl phthalate is added to the azeotropic extraction and rectification tower, and the temperature at the top and bottom of the tower is controlled for azeotropic extraction and rectification. , toluene and water mixed gas are obtained at the top of the tower, and a mixture of DMF and modified extractant is obtained at the bottom of the tower; after condensation, the mixed gas of toluene and water is divided into a toluene layer with a content of more than 99% and a water layer with a toluene content of less than 0.08% The mixture of DMF and modified extractant is processed by rectification in the solvent regeneration circulation tower, and more than 99.9% of DMF is obtained at the top of the tower, and the modified extractant is obtained at the bottom of the solvent regeneration circulation tower, which is circulated to the azeotropic extraction rectification tower.
Description
Technical field
The present invention relates to the integrated technique that a kind of multicomponent mixture separates, be specifically related to a kind of azeotropic extraction rectifying and the liquid liquid stratified set composition method from sodium salt-dimethyl formamide-toluene-water mixed solution.
Background technology
Dimethyl formamide (be called for short: DMF) and toluene be important industrial chemicals and solvent, be widely used in pharmacy and pesticide intermediate building-up process, in pharmacy and pesticide intermediate building-up process, adopt above-mentioned solvent, easily form the mixing solutions of sodium salt, DMF, toluene and water.Mainly contain physico-chemical process, biochemical process and chemical hydrolysis for recovery and the treatment process containing sodium salt, DMF and toluene in waste water both at home and abroad at present.Adopt biochemical process and chemical hydrolysis all can destroy DMF and toluene structure.The biochemical process treatment time is long, degraded is not thorough, and in addition, DMF can make microorganism poisoning, and biological treatment is caused to very big impact; Chemical method does not reach the object that reclaims DMF and toluene, easily causes secondary pollution.
As taked effective separation method, not only can reclaim DMF and toluene to above-mentioned mixed solution, reach the object of processing waste water simultaneously, reduce treating processes cost.Adopt low boiling point solvent as CH
2cl
2, chloroform, dichlorobenzene, benzene, pimelinketone or methyl-phenoxide etc. carry out liquid-liquid extraction as extraction agent, recyclable DMF, but need further to separate containing the mixed solvent of extraction agent after extraction, reaches 1～3% containing organic solvent in water after separating, and easily causes secondary pollution.For high density DMF and toluene (nearly 100 g/L) waste water, distillation method separate DMF, toluene and water, the DMF of recovery and toluene can be back to production, but separate after waste water COD reach 40000PPM, process energy consumption is higher; If DMF and toluene mass concentration are lower than 50 g/L in waste water, this method cost recovery will increase considerably, very uneconomical.Absorption method has the features such as technical process is short, simple to operate, recovering effect is good, but mixing organism after absorption needs further to process, and adsorbent reactivation needs high energy consumption.
Summary of the invention
The object of the present invention is to provide a kind of azeotropic extraction rectifying and the liquid liquid stratified set composition technique from sodium salt, DMF, toluene and water mixed solution, compared with traditional technology, it is fairly simple that the present invention has processing step, through flash liberation, content, the yield of DMF and toluene are higher, and after separating, the COD of water is lower than 800PPM; Extraction agent used is convenient to regeneration and recycle, and sepn process energy consumption is low.
For achieving the above object, the present invention adopts following technical scheme:
Azeotropic extraction rectifying and liquid liquid stratified set composition, from a method for sodium salt-DMF-toluene-water mixed solution, comprise the following steps:
1) after raw material sodium salt, DMF, toluene and water mixed solution preheating, again by the desalination of desalination evaporating pot, mixing solutions after desalination adds azeotropic extraction rectifying tower from the middle and lower part of azeotropic extraction rectifying tower, modification extraction agent is added in azeotropic extraction rectifying tower by the middle and upper part of azeotropic extraction rectifying tower, and described modification extraction solvent is the mixed solvent of tetramethylene sulfone and dioctyl phthalate (DOP); Control tower top, column bottom temperature, mixing solutions is at azeotropic extraction rectifying tower through azeotropic extraction rectifying, and tower top obtains toluene and water mixing gas, obtains the mixture of DMF and modification extraction agent at the bottom of tower;
2) toluene and water mixing gas, after condensation, are divided into toluene layer and water layer, and toluene layer is containing the toluene of more than 99% (mass content, below content be mass content), and water layer toluene level is lower than 0.08%; Toluene is partly refluxed to azeotropic extraction rectifying tower;
3) mixture of DMF and modification extraction agent is through solvent reclamation recycle column rectification process, and solvent reclamation recycle column tower top obtains 99.9% DMF, at the bottom of solvent reclamation recycle column tower, obtains modification extraction agent, is circulated to azeotropic extraction rectifying tower.
The inventive method has been set up a kind of azeotropic extraction rectificating method, and traditional azeotropic distillation and extracting rectifying effective integration, in same device, are realized to separating of DMF, toluene and water on same azeotropic extraction rectifying tower, has simplified the technological process of production.
In described method, the temperature at the bottom of tower top and the tower of azeotropic extraction rectifying tower is respectively 83.8～84.5 ℃ and 95.7～97.5 ℃.
In described method, the mass ratio of raw material and modification extraction agent is 1:0.4～1.0.
In described method, described modification extraction solvent is the sulfolane solution containing 15～20% dioctyl phthalate (DOP)s.
In described method, mixing solutions and azeotropic extractive distillation column overhead vapours carry out heat exchange and carry out preheating.
Azeotropic extraction rectifying of the present invention and liquid liquid stratified set composition are from sodium salt, DMF, the method of toluene and water mixed solution, concrete steps are as follows: sodium salt, DMF, toluene and water mixed solution are 1. through azeotropic extraction rectifying tower tower top steam preheating, again by after the desalination of desalination evaporating pot, added in azeotropic extraction rectifying tower by the middle and lower part of azeotropic extraction rectifying tower, azeotropic extraction rectifying tower tower top, column bottom temperature is respectively 83.8～84.5 ℃ and 95.7～97.5 ℃, 6. modification extraction agent (adds 15-20wt% dioctyl phthalate (DOP)) in the upper position charging of azeotropic extraction rectifying tower in tetramethylene sulfone, after azeotropic distillation and extracting rectifying, 3. azeotropic extraction rectifying tower tower top is the mixing gas of toluene and water, after raw material condensation (with the 1. heat exchange of charging mixing solutions) and cryogenic condensation, ℃ (raw material condensation effectively utilizes the heat of azeotropic extraction rectifying tower tower top gas in fluid temperature≤20, cryogenic condensation guarantees that tower top gas is condensed into liquid), be divided into toluene layer 4. with water layer 5., 4. toluene layer is 99.5% above toluene, 5. water layer is more than 99.9% water (toluene is lower than 0.08%), it at the bottom of azeotropic extraction rectifying tower, is 8. the mixed solution of modification extraction agent and DMF, mixed solution is 8. through solvent reclamation recycle column rectification process, 7. solvent reclamation circulation tower top distillates cut is more than 99.9% DMF solution, and at the bottom of tower, discharging is that modification extraction agent is circulated to azeotropic extraction rectifying tower, recycles.
The preferred processing condition of described sepn process are as follows: in sepn process, each tower reactor, tower top temperature control, reflux ratio, feed entrance point and stage number are shown in Table 1.
Table 1 sepn process processing condition
The present invention adopts azeotropic extraction rectifying and the liquid liquid stratified set composition technique from sodium salt-DMF-toluene-water mixed solution, by traditional azeotropic distillation and extracting rectifying effective integration in same device, on same azeotropic extraction rectifying tower, realize separating of DMF, toluene and water, simplified the technological process of production.Compared with traditional technology, the inventive method, by traditional azeotropic distillation and extracting rectifying effective integration, adopts desalter to carry out preheating and desalination, realizes polycomponent and separate in azeotropic extraction rectifying tower, and technological process is simple; Adopt azeotropic extraction rectifying tower tower top steam to raw material preheating, effectively utilize heat, reduce energy consumption; Adopt modification extraction solvent, significantly reduce the fusing point of extraction agent, while avoiding winter environment temperature low, on the impact of azeotropic extraction rectifying.Described method stock liquid, through azeotropic extraction rectifying and the primary treatment of liquid liquid stratified set apparatus for converting, once can obtain more than 99.5% toluene and 99.9% above DMF, more than one time yield all reaches 98 %, after separating, in water, contains toluene lower than 0.08%.
Accompanying drawing explanation
Fig. 1 is azeotropic extraction rectifying and the liquid liquid stratified set composition process flow diagram from sodium salt-DMF-toluene-water mixed solution.
Embodiment
Azeotropic extraction rectifying of the present invention and liquid liquid stratified set composition are from the method for sodium salt, DMF, toluene and water mixed solution, tripping device and technical process are with reference to Fig. 1, and wherein 1 is azeotropic extraction rectifying tower, and 2 is desalter, 3 is azeotropic extraction rectifying tower well heater, 4 is feed preheater, and 5 is subcooling condenser, and 6 is venting hole, 7 is liquid liquid layering tank, 8 is condenser, and 9 is solvent reclamation recycle column, and 10 is well heater.
Adopting sodium salt, DMF, toluene and the water mixed solution that certain company provides is raw material, operating under normal pressure of azeotropic extraction rectifying tower carried out, tower internal diameter is 50mm, the Stainless Steel Helices of in-built φ 3*3 θ type, through measuring by standards system, this height equivalent to one theoretical plate HETP=27mm, tower reactor heats with electric mantle, raw material, modification extractant feed and discharging are all with glass rotameter metering, and azeotropic extraction rectifying tower and solvent reclamation recycle column all adopt external reflux.
Sodium salt, DMF, toluene and water mixed solution 1. in feed preheater 4 through the 1 overhead vapours preheating of azeotropic extraction rectifying tower, and then by 2 desalinations of desalination evaporating pot, added in azeotropic extraction rectifying tower 1 by the middle and lower part of azeotropic extraction rectifying tower 1, azeotropic extraction rectifying tower 1 tower top, column bottom temperature is respectively 83.8～84.5 ℃ and 95.7～97.5 ℃, 6. modification extraction agent (adds 15-20% dioctyl phthalate (DOP)) in the upper position charging of azeotropic extraction rectifying tower 1 in tetramethylene sulfone, 1. raw material is 1:0.4～1.0 with the ratio of modification extraction agent, 3. azeotropic extraction rectifying tower 1 tower top material is the mixing gas of toluene and water, after feed preheater 4 and subcooling condenser 5 raw material condensations and cryogenic condensation, tower top gas is condensed into liquid, fluid temperature≤20 ℃, in liquid liquid layering tank 7, be divided into toluene layer 4. with water layer 5., 4. toluene layer is 99.5% above toluene, 5. water layer is 99.9% water (toluene is lower than 0.08%), 8. azeotropic extraction rectifying tower 1 materials at bottom of tower is the mixed solution of modification extraction agent and DMF, tower reactor mixed solution is sent into solvent reclamation recycle column 9, process through solvent reclamation recycle column 9,7. solvent reclamation recycle column 9 tower tops distillate cut is more than 99.9% DMF solution, materials at bottom of tower is modification extraction agent, be circulated to azeotropic extraction rectifying tower 1, recycle.
The processing condition of sepn process: in sepn process, the control of each tower reactor temperature, reflux ratio, feed entrance point and stage number are shown in Table 1.
Analyze through HP chromatographic instrument, raw material and each fractions consisting detailed results are shown in Table 2.
The rectifying of table 2 azeotropic extraction and liquid liquid stratified set composition are from the separating resulting of sodium salt, DMF, toluene and water mixed solution
Claims (6)
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104874196A (en) * | 2015-03-26 | 2015-09-02 | 南京师范大学 | Method for processing sodium and ammonium acetate-diazonium organic compound-methanol-water mixed solution |
| CN105017054A (en) * | 2015-07-07 | 2015-11-04 | 天津大学 | Solvent recovering system for DMF (Dimethyl Formamide) saliferous wastewater |
| CN105348035A (en) * | 2015-12-15 | 2016-02-24 | 南京师范大学 | Method for integrated purification of chloroform and ethyl acetate mixed solution through azeotropic extractive distillation and liquid-liquid delamination |
| US10370398B2 (en) | 2016-06-23 | 2019-08-06 | Tate & Lyle Technology Limited | Liquid-liquid extraction of DMF |
| CN114276269A (en) * | 2021-12-29 | 2022-04-05 | 烟台国邦化工机械科技有限公司 | Recycling treatment method for wastewater in fiber production |
| CN115724708A (en) * | 2022-12-29 | 2023-03-03 | 南京长江江宇环保科技股份有限公司 | Method for separating toluene and N, N-dimethylformamide mixture |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101709025A (en) * | 2009-11-03 | 2010-05-19 | 南京师范大学 | Compound cross-flow liquid-liquid extraction separation method of methylal-methanol azeotropic system |
| CN101734998A (en) * | 2009-12-22 | 2010-06-16 | 南京师范大学 | Method for extracting trimethylbenzene fraction in hydrocracking C9 by combined solvent extraction rectification method |
-
2014
- 2014-02-13 CN CN201410049816.3A patent/CN103772230B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101709025A (en) * | 2009-11-03 | 2010-05-19 | 南京师范大学 | Compound cross-flow liquid-liquid extraction separation method of methylal-methanol azeotropic system |
| CN101734998A (en) * | 2009-12-22 | 2010-06-16 | 南京师范大学 | Method for extracting trimethylbenzene fraction in hydrocracking C9 by combined solvent extraction rectification method |
Non-Patent Citations (1)
| Title |
|---|
| G. SARAVANAN ET AL.: "Liquid-Liquid Equilibria for the System Ethyl Acetate-Acetic Acid-Water in the Presence of Dissolved Inorganic Salts", 《JOURNAL OF CHEMICAL AND ENGINEERING DATA》 * |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104874196A (en) * | 2015-03-26 | 2015-09-02 | 南京师范大学 | Method for processing sodium and ammonium acetate-diazonium organic compound-methanol-water mixed solution |
| CN104874196B (en) * | 2015-03-26 | 2016-09-14 | 南京师范大学 | A kind of method for processing sodium and ammonium acetate-diazonium organic matter-methanol-water mixed solution |
| CN105017054A (en) * | 2015-07-07 | 2015-11-04 | 天津大学 | Solvent recovering system for DMF (Dimethyl Formamide) saliferous wastewater |
| CN105017054B (en) * | 2015-07-07 | 2017-01-11 | 天津大学 | Solvent recovering system for DMF (Dimethyl Formamide) saliferous wastewater |
| CN105348035A (en) * | 2015-12-15 | 2016-02-24 | 南京师范大学 | Method for integrated purification of chloroform and ethyl acetate mixed solution through azeotropic extractive distillation and liquid-liquid delamination |
| CN105348035B (en) * | 2015-12-15 | 2017-05-17 | 南京师范大学 | Method for integrated purification of chloroform and ethyl acetate mixed solution through azeotropic extractive distillation and liquid-liquid delamination |
| US10370398B2 (en) | 2016-06-23 | 2019-08-06 | Tate & Lyle Technology Limited | Liquid-liquid extraction of DMF |
| US10899783B2 (en) | 2016-06-23 | 2021-01-26 | Tate & Lyle Technology Limited | Liquid-liquid extraction of DMF |
| CN114276269A (en) * | 2021-12-29 | 2022-04-05 | 烟台国邦化工机械科技有限公司 | Recycling treatment method for wastewater in fiber production |
| CN115724708A (en) * | 2022-12-29 | 2023-03-03 | 南京长江江宇环保科技股份有限公司 | Method for separating toluene and N, N-dimethylformamide mixture |
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| CN103772230B (en) | 2016-01-27 |
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