CN1793111A - Process for recovering dimethyl formyl amide from waste water - Google Patents
Process for recovering dimethyl formyl amide from waste water Download PDFInfo
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- CN1793111A CN1793111A CN 200510086784 CN200510086784A CN1793111A CN 1793111 A CN1793111 A CN 1793111A CN 200510086784 CN200510086784 CN 200510086784 CN 200510086784 A CN200510086784 A CN 200510086784A CN 1793111 A CN1793111 A CN 1793111A
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- dimethyl formamide
- waste water
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- rectifying
- dmf
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- 238000000034 method Methods 0.000 title claims abstract description 43
- 239000002351 wastewater Substances 0.000 title claims abstract description 27
- -1 dimethyl formyl amide Chemical compound 0.000 title description 2
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 claims abstract description 204
- 238000000605 extraction Methods 0.000 claims abstract description 31
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 239000003960 organic solvent Substances 0.000 claims description 21
- 238000000926 separation method Methods 0.000 claims description 17
- 238000000746 purification Methods 0.000 claims description 15
- 238000007670 refining Methods 0.000 claims description 12
- 150000007530 organic bases Chemical class 0.000 claims description 7
- 238000000638 solvent extraction Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 238000004821 distillation Methods 0.000 claims description 6
- 230000002378 acidificating effect Effects 0.000 claims description 4
- 239000007864 aqueous solution Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000012535 impurity Substances 0.000 abstract description 8
- 239000002253 acid Substances 0.000 abstract 1
- 239000003513 alkali Substances 0.000 abstract 1
- 230000003247 decreasing effect Effects 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 20
- 238000005265 energy consumption Methods 0.000 description 11
- 230000008901 benefit Effects 0.000 description 8
- 239000012071 phase Substances 0.000 description 8
- 239000007787 solid Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 239000002904 solvent Substances 0.000 description 5
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 241000282326 Felis catus Species 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000010985 leather Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 239000012074 organic phase Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical group C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- NSOXQYCFHDMMGV-UHFFFAOYSA-N Tetrakis(2-hydroxypropyl)ethylenediamine Chemical compound CC(O)CN(CC(C)O)CCN(CC(C)O)CC(C)O NSOXQYCFHDMMGV-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000622 liquid--liquid extraction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- WHQSYGRFZMUQGQ-UHFFFAOYSA-N n,n-dimethylformamide;hydrate Chemical compound O.CN(C)C=O WHQSYGRFZMUQGQ-UHFFFAOYSA-N 0.000 description 2
- 239000004814 polyurethane Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- UOCLXMDMGBRAIB-UHFFFAOYSA-N 1,1,1-trichloroethane Chemical compound CC(Cl)(Cl)Cl UOCLXMDMGBRAIB-UHFFFAOYSA-N 0.000 description 1
- LIPPKMMVZOHCIF-UHFFFAOYSA-N 1,1,2-trichloroprop-1-ene Chemical compound CC(Cl)=C(Cl)Cl LIPPKMMVZOHCIF-UHFFFAOYSA-N 0.000 description 1
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 1
- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- HPNMFZURTQLUMO-UHFFFAOYSA-N diethylamine Chemical compound CCNCC HPNMFZURTQLUMO-UHFFFAOYSA-N 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000004434 industrial solvent Substances 0.000 description 1
- 239000002649 leather substitute Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- SNMVRZFUUCLYTO-UHFFFAOYSA-N n-propyl chloride Chemical compound CCCCl SNMVRZFUUCLYTO-UHFFFAOYSA-N 0.000 description 1
- 229920002239 polyacrylonitrile Polymers 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000004448 titration Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a recycle method for dimethyl formamide from waste water. The feature is that it contains two processes of extraction and rectification. The acid impurity could be neutralized by organic alkali to avoid the corruption to the device. The power consumption is decreased, and the process is simple. The purity of dimethyl formamide could be 99.9% and the recovery rate could reach to 98.5%.
Description
Technical field
The present invention relates to the recovery method of solvent, particularly relate to extraction, the rectifying combination technique recovery method of the dimethyl formamide (DMF) in a kind of waste water, belong to the separating and purifying technology field of dimethyl formamide.
Background technology
N, dinethylformamide is called for short DMF, is a kind of good industrial solvent and organic synthesis material, is widely used in a lot of industries, wherein mainly contains: 1) polyacrylonitrile fibre spinning solvent; 2) in petrochemical complex as gas absorbent, the selectivity that is used for acetylene absorbs and the separation and purification of C4 such as divinyl; 3) in leatheroid production, be used as solvent.How the corresponding waste water that contains DMF in a large number that produced of these application processes reclaims DMF wherein cost-effectively and handles the waste water of following, and all is very important for raising enterprise whole economic efficiency, social benefit.
Specifically concerning the synthetic leather industry, DMF is a large amount of solvents that use of wet polyurethane (PU) leather factory, being mainly used in the batching dilution, wait to finish process of setting and soluble in water after utilize supporting device that DMF is reclaimed circulation again to reuse.At present, general directly by rectificating method the DMF-water sepn is come abbreviates water law as in the industrial practice.The shortcoming of water law is a technological process energy consumption height, and heat energy consumption accounts for more than 80% of DMF cost recovery, especially is not suitable for to contain the lower rare liquid waste disposal of DMF concentration.Domestic wet method is moved the interior DMF of waste liquid that discharges in the hymeniderm leather production process, and often concentration is very low, as uses domestic simple DMF water law retrieving arrangement at present, because the energy consumption height, recycling expense costliness makes factory not have direct economic benefit.If the DMF waste liquid directly is discharged in the external environment, is not only loss economically, and causes serious environmental to pollute.
Over past ten years, China PU leather industry development is swift and violent, producing competition is growing more intense, energy-conservation and environmental protection has become a very important problem, and the sector concentrates on scarce coal area, south mostly, year, quota of expenditure coal number was huge, if unit consumption of energy is declined to a great extent, annual producible direct economic benefit will be very considerable.
Summary of the invention
The present invention handles the particularly shortcoming that energy consumption is big, economic benefit is low that had of lower concentration DMF of DMF in the waste water, the method for DMF in a kind of new recovery waste water of proposition of reclaiming at traditional water law.This method at first is extracted into the DMF in the waste water in the organic phase by solvent extraction, by rectificating method organic solvent is separated with DMF then, obtains pure DMF product.
The invention provides the recovery method of dimethyl formamide in a kind of waste water, it is characterized in that: this method mainly comprises extraction and two operations of rectifying, at first adopt organic solvent extraction, dimethyl formamide in the aqueous solution is transferred in the organic solvent, and then realized separating of dimethyl formamide and organic solvent by rectifying.
Furtherly, the rectifying separation operation of described organic solvent and dimethyl formamide is divided into two sections of initial gross separation and refining purifying, and wherein the rectifying mode that adopts of initial gross separation is an atmospheric distillation, and the rectifying mode that refining purifying adopts is rectification under vacuum.
In the present invention, the refining purification section of the rectifying separation operation of described organic solvent and dimethyl formamide adopts the mode extraction dimethyl formamide of side line gas phase discharging.
In purification column, add organic bases in described refining purification phase,, reduce the corrodibility of system with the acidic substance that produce in the N-process.
In the present invention, described extraction process equipment can adopt packed extraction tower.
The invention has the beneficial effects as follows:
1) whole Separation and Recovery process energy consumption reduces greatly.The present invention adopt the organic solvent extraction technology with DMF with become separating of DMF and organic solvent separating of water.Extraction process carries out at normal temperatures, and energy consumption is low, with treatment scale 1m
3/ hr is an example, need power consumption 0.75 degree/hour.Selected organic extractant separates with DMF than easier with water, and the vaporization heat of organic extractant is about 1/8 of water, with DMF boiling-point difference bigger (more than or equal to 80 ℃), the progression that sepn process needs is few, reflux ratio is low, and steam consumption significantly reduces, and energy consumption obviously reduces.With 1m
3The waste water of/hr (DMF 10%) treatment scale is an example, and the entire treatment device only needs 1 ton of 8 kilograms of boiler as power, and usage load is about original 60%;
2) inorganic salts in the waste water, solid substance are the problems that must consider in traditional water law treating processes, and these impurity are separated out in rectifying workshop section vaporizer easily, fouling, thereby cause the obstruction of vaporizer tubulation, are difficult to cleaning, have a strong impact on operation.Because novel method adopts the organic solvent extracting taking technique, the mineral-type impurity in the waste water comprises that solid substance all discharges with water, thereby has significantly reduced in the conventional processes that impurity enters in the rectification working process and the rectifying tower reboiler stopping state that produces.
3) because rectification working process divides two sections of initial gross separation and refining purifying, the rectifying mode that wherein refining purifying is adopted is rectification under vacuum, to reduce the service temperature of sepn process, make the whole recovery process temperature be no more than 130 ℃, significantly reduce the decomposition of DMF and system to the corrosive nature of separating device material, also improved heat utilization efficiency.
Utilize the purity of the DMF of the method for the invention recovery can reach 99.9%; the rate of recovery can reach 98.5%; economy with respect to water law is better; thereby can handle the DMF waste water of lower concentration; it is also lucrative that feasible processing is lower than the DMF waste liquid of 10% concentration; under the situation that the international energy price is more and more high and environment protection becomes more and more important at present, its application prospect is very wide.
Description of drawings
Fig. 1 is the FB(flow block) of an embodiment of the method for the invention.
Embodiment
The invention provides the recovery method of dimethyl formamide in a kind of waste water (DMF), this method mainly comprises extraction and two operations of rectifying, at first adopt organic solvent extraction, the DMF in the aqueous solution is transferred in the organic solvent, and then realize separating of DMF and organic solvent by rectifying.Extraction agent selects to satisfy the organic solvent of following character: with DMF good consistency (being generally miscible) is arranged 1.; 2. the consistency with water very low (solubleness in water<1%); 3. with boiling-point difference 〉=80 of DMF ℃.The solvent of Chang Xuan such as chloroform, tetracol phenixin, 1,1 ethylene dichloride, 1,1,1 trichloroethane, 1,2 Ethylene Dichloride, chloropropane and tri chloropropene etc.The rectifying separation operation of described organic solvent and dimethyl formamide is divided into two sections of initial gross separation and refining purifying, and wherein the rectifying mode that adopts of initial gross separation is an atmospheric distillation, and the rectifying mode that refining purifying adopts is rectification under vacuum.The smart vacuum pressure value of slipping of decompression can be-0.04~-0.07MPa between, vacuum tightness is too little, does not have to reduce smart effect of slipping temperature in the tower, vacuum tightness too greatly then increases loss of extractant and vacuum energy consumption.
The present invention is implemented as follows: at first lower concentration DMF waste water (mass percent concentration≤10%) is fed extraction tower, waste water carries out the exchange of liquid-liquid extraction mass transfer with the organic solvent of respective streams ratio in extraction tower, DMF enters the organic extraction phase by water, and impurity such as solid substance is then stayed water (extracting phase) in the waste water.The organic extraction that contains DMF then enters the rectifying separation operation mutually.The rectifying separation operation is divided two sections, promptly realizes the upgrading tower of initial gross separation and the purification column that realizes making with extra care purifying.Upgrading tower is the atmospheric distillation tower, and extraction phase is condensed into the organic solution that contains about DMF50% therein.At last concentrated solution is fed the DMF purification column, purification column is the rectification under vacuum tower, reaches the reduction rectification temperature by decompression, reduces system component and decomposes and the corrosive purpose.Purity be 99.9% DMF by the extraction of side line gas phase, can obtain the finished product after the condensation.
The acidic impurities that produces in the recovery technological process of the present invention utilizes organic bases (as quadrol, diethylamine etc.) to react neutralization, organic bases from purification column bottom side line continuously by being metered into.The degree of DMF hydrolysis can judge indirectly and obtain by regularly the potential of hydrogen of system rectifying tower still being carried out titration, and the add-on of definite organic bases thus.
Because the method for the invention earlier is transferred to organic phase with DMF by water by the less energy-consumption extraction process, by rectifying organic extractant is separated with DMF then, therefore whole process is compared energy consumption with traditional water law and is reduced greatly.Especially for DMF concentration less than 10% waste water, the water more than 90% need be steamed during with traditional water law recovery, energy consumption is huge, from becoming unreasonable economically, and with the obvious advantage with the method for the invention, can obtain economy and environment economic benefits and social benefits benefit.
Below in conjunction with accompanying drawing a specific embodiment of the present invention is described.
As shown in Figure 1, the DMF aqueous solution of 10% (mass percent concentration) is entered gently inlet mutually of filler extraction tower bottom with 1.0 tons/hour flow, organic solvent (chloroform) enters heavy liquid inlet, extraction tower top with 2 tons/hour flow, and organic phase and water carry out the exchange of liquid-liquid extraction mass transfer in extraction tower.Contain DMF concentration and be 5% organic extraction and feed upgrading tower by the extraction tower heavy out.Waste water flows out from the cat head light phase export, discharging after extraction agent reclaims and further handles.Upgrading tower is an atmospheric distillation, and the still temperature is 95 ℃, and reflux ratio is 0.2.The organic solution of organic extraction simmer down to DMF concentration about 50% in upgrading tower is by discharging at the bottom of the tower.It is that extraction agent is back to extraction process that concentrated cat head distillates component.DMF concentration is to enter purification column after 50% organic solution is discharged from the upgrading tower bottom.Purification column is the rectification under vacuum tower, and vacuum is-0.05MPa that tower still temperature is 130 ℃.
Organic solution obtains separating by rectification under vacuum in this tower, and cat head returns the upgrading tower inlet for containing the organic extractant of a small amount of DMF (<1%).Purity reach 99.9% DMF with the gas phase form from the side line extraction, after condensation, obtain the finished product.
Reclaim the acidic impurities that produces in the technological process and utilize the organic bases quadrol to react neutralization, organic bases from purification column bottom side line continuously by being metered into.The small molecules resin impurity that enters distillation system in a spot of solid substance in the system (most solid substances enter raffinate item aqueous phase in the waste water in extraction process, discharge with water), the waste water is regularly discharged from the purification column bottom by thermogenetic viscous fluid and acid-base neutralisation product etc.
Claims (5)
1. the recovery method of dimethyl formamide in the waste water, it is characterized in that: this method mainly comprises extraction and two operations of rectifying, at first adopt organic solvent extraction, dimethyl formamide in the aqueous solution is transferred in the organic solvent, and then realized separating of dimethyl formamide and organic solvent by rectifying.
2. the recovery method of dimethyl formamide in the waste water according to claim 1, it is characterized in that: the rectifying separation operation of described organic solvent and dimethyl formamide is divided into two sections of initial gross separation and refining purifying, wherein the rectifying mode of initial gross separation employing is an atmospheric distillation, and the rectifying mode that refining purifying adopts is rectification under vacuum.
3. the recovery method of dimethyl formamide in the waste water according to claim 1 is characterized in that: the refining purification section of the rectifying separation operation of described organic solvent and dimethyl formamide adopts the mode extraction dimethyl formamide of side line gas phase discharging.
4. the recovery method of dimethyl formamide in the waste water according to claim 1 is characterized in that: add organic bases in described refining purification phase in purification column, with the acidic substance that produce in the N-process, reduce the corrodibility of system.
5. the recovery method of dimethyl formamide in the waste water according to claim 1 is characterized in that: described extraction process equipment adopts packed extraction tower.
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CNB2005100867845A CN1317259C (en) | 2005-11-04 | 2005-11-04 | Process for recovering dimethyl formyl amide from waste water |
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CNB2005100867845A CN1317259C (en) | 2005-11-04 | 2005-11-04 | Process for recovering dimethyl formyl amide from waste water |
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CN1317259C CN1317259C (en) | 2007-05-23 |
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Cited By (20)
Publication number | Priority date | Publication date | Assignee | Title |
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CN101792221A (en) * | 2010-04-09 | 2010-08-04 | 安徽南风环境工程技术有限公司 | Method for pre-treating N,N-dimethylformamide-containing waste water |
CN102408349A (en) * | 2011-11-19 | 2012-04-11 | 无锡双象超纤材料股份有限公司 | System for removing formic acid generated during dimethylformamide recovering process |
CN101397260B (en) * | 2008-11-19 | 2012-06-27 | 河北工业大学 | Technology for recovering dimethylformamide from waste water by combination of saline extraction and rectification method |
CN102557355A (en) * | 2012-02-15 | 2012-07-11 | 蒋梦琪 | Treatment method of wastewater containing amino compounds by copolymerization and extraction |
CN104003566A (en) * | 2014-05-28 | 2014-08-27 | 东莞市灿森新材料有限公司 | Method for recovering multi-component liquid waste in process of producing high-performance aramid fibrid |
CN104384172A (en) * | 2014-10-25 | 2015-03-04 | 陈列鑫 | Disposal method for rectification residues in production of synthetic leather |
CN104844433A (en) * | 2015-01-07 | 2015-08-19 | 青岛科技大学 | Method for separating acetone/DMF/water ternary system by rectifying through high- and low- pressure towers |
CN106397252A (en) * | 2016-08-31 | 2017-02-15 | 山东普洛得邦医药有限公司 | Device and method for efficiently recovering DMF (N,N-dimethylformamide) from waste water |
CN106565524A (en) * | 2016-09-22 | 2017-04-19 | 南通万顺化工科技有限公司 | A method of recovering dimethyl formamide |
CN106748864A (en) * | 2016-12-27 | 2017-05-31 | 广东创源节能环保有限公司 | The technique that a kind of double heat pump distillation methods of low pressure economic benefits and social benefits process DMF waste water |
CN107215994A (en) * | 2017-06-16 | 2017-09-29 | 山东康宝生化科技有限公司 | A kind of method for concentrating the dilute DMF waste water of Sucralose |
CN108059291A (en) * | 2017-10-26 | 2018-05-22 | 淄博鑫泉医药技术服务有限公司 | The recovery method of DMF and inorganic salts in cefotaxime side chain acid esters waste water |
CN108774148A (en) * | 2018-07-11 | 2018-11-09 | 刘志 | A kind of PU synthetic leather wet method prepare in the recovery and treatment method of solvent |
CN108793553A (en) * | 2018-06-09 | 2018-11-13 | 石家庄市绿丰化工有限公司 | A kind of method of DMF Sewage treatments |
CN108862795A (en) * | 2018-07-16 | 2018-11-23 | 兰博尔开封科技有限公司 | The synthetical recovery processing method of DMF in a kind of cyazofamid waste water |
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CN111470997A (en) * | 2020-04-26 | 2020-07-31 | 安庆市鑫祥瑞环保科技有限公司 | Method for recovering DMF waste liquid |
CN112479919A (en) * | 2020-11-30 | 2021-03-12 | 安徽金禾实业股份有限公司 | Method for recovering dilute DMF (dimethyl formamide) in sucralose crystallization mother liquor wastewater |
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CN101397260B (en) * | 2008-11-19 | 2012-06-27 | 河北工业大学 | Technology for recovering dimethylformamide from waste water by combination of saline extraction and rectification method |
CN101792221A (en) * | 2010-04-09 | 2010-08-04 | 安徽南风环境工程技术有限公司 | Method for pre-treating N,N-dimethylformamide-containing waste water |
CN101792221B (en) * | 2010-04-09 | 2011-07-20 | 安徽南风环境工程技术有限公司 | Method for pre-treating N,N-dimethylformamide-containing waste water |
CN102408349A (en) * | 2011-11-19 | 2012-04-11 | 无锡双象超纤材料股份有限公司 | System for removing formic acid generated during dimethylformamide recovering process |
CN102408349B (en) * | 2011-11-19 | 2014-07-02 | 无锡双象超纤材料股份有限公司 | System for removing formic acid generated during dimethylformamide recovering process |
CN102557355A (en) * | 2012-02-15 | 2012-07-11 | 蒋梦琪 | Treatment method of wastewater containing amino compounds by copolymerization and extraction |
CN104003566A (en) * | 2014-05-28 | 2014-08-27 | 东莞市灿森新材料有限公司 | Method for recovering multi-component liquid waste in process of producing high-performance aramid fibrid |
CN104384172A (en) * | 2014-10-25 | 2015-03-04 | 陈列鑫 | Disposal method for rectification residues in production of synthetic leather |
CN104844433A (en) * | 2015-01-07 | 2015-08-19 | 青岛科技大学 | Method for separating acetone/DMF/water ternary system by rectifying through high- and low- pressure towers |
CN104844433B (en) * | 2015-01-07 | 2016-09-21 | 青岛科技大学 | A kind of method of high-low pressure double-tower rectification acetone/DMF/ water ternary system |
CN106397252A (en) * | 2016-08-31 | 2017-02-15 | 山东普洛得邦医药有限公司 | Device and method for efficiently recovering DMF (N,N-dimethylformamide) from waste water |
CN106565524A (en) * | 2016-09-22 | 2017-04-19 | 南通万顺化工科技有限公司 | A method of recovering dimethyl formamide |
CN106748864A (en) * | 2016-12-27 | 2017-05-31 | 广东创源节能环保有限公司 | The technique that a kind of double heat pump distillation methods of low pressure economic benefits and social benefits process DMF waste water |
CN106748864B (en) * | 2016-12-27 | 2019-02-05 | 广东创源节能环保有限公司 | A kind of technique of the double heat pump distillation method processing DMF waste water of low pressure economic benefits and social benefits |
CN107215994A (en) * | 2017-06-16 | 2017-09-29 | 山东康宝生化科技有限公司 | A kind of method for concentrating the dilute DMF waste water of Sucralose |
CN108059291B (en) * | 2017-10-26 | 2020-09-04 | 山东鑫泉医药有限公司 | Method for recovering DMF (dimethyl formamide) and inorganic salt in ceftazidime side chain acid ester wastewater |
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CN108793553A (en) * | 2018-06-09 | 2018-11-13 | 石家庄市绿丰化工有限公司 | A kind of method of DMF Sewage treatments |
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