CN1793111A - Process for recovering dimethyl formyl amide from waste water - Google Patents

Process for recovering dimethyl formyl amide from waste water Download PDF

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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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distillation
dimethylformamide
wastewater
dmf
organic solvent
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CN 200510086784
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CN1317259C (en )
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杨明德
吴玉龙
党杰
胡湖生
王欣昌
何培炯
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清华大学
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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

一种废水中二甲基甲酰胺的回收方法 The method for recovering wastewater dimethylformamide

技术领域 FIELD

本发明涉及溶剂的回收方法,特别是涉及一种废水中的二甲基甲酰胺(DMF)的萃取、精馏组合技术回收方法,属于二甲基甲酰胺的分离纯化技术领域。 The present invention relates to the recovery of the solvent, particularly to a waste water extraction in dimethyl formamide (DMF), the distillation recovery methods combining techniques, purification techniques belonging to the field of separation of dimethyl formamide.

背景技术 Background technique

N,N-二甲基甲酰胺简称DMF,是一种优良的工业溶剂和有机合成材料,广泛应用于很多行业,其中主要有:1)聚丙烯腈纤维纺丝用溶剂;2)在石油化工中作为气体吸收剂,用于乙炔的选择性吸收和丁二烯等C4的分离精制;3)在人造革生产中用作溶剂。 N, N- dimethylformamide abbreviation of DMF, is an excellent industrial solvent and organic synthetic materials are widely used in many industries, which are: 1) a solvent for polyacrylonitrile fiber spinning; 2) in the petrochemical industry as a gas absorbent for the selective absorption of acetylene and butadiene, C4 separation and purification; and 3) was used as a solvent in the production of artificial leather. 这些应用过程相应产生了大量含DMF的废水,如何经济有效地回收其中的DMF并处理伴随的废水,对于提高企业整体经济效益、社会效益都是非常重要的。 The application process accordingly generated a lot of waste water containing DMF, how to cost-effectively recover one of the DMF and associated waste water treatment, to improve the overall economic efficiency of enterprises and social benefits are very important.

具体对合成革行业来说,DMF是湿法聚氨酯(PU)革厂大量使用的溶剂,主要用于配料稀释,待完成凝固过程并溶于水中后再利用配套的装置将DMF回收起来循环重复使用。 Specific synthetic leather industry, the solvent is DMF wet polyurethane (PU) tannery extensive use, primarily for dilution ingredients until complete solidification process and dissolved in water before use supporting means up cycle was repeated using the recovered DMF . 目前,工业实践中一般直接通过精馏方法将DMF-水分离开来,简称为水法。 Currently, commercial practice generally be directly separated from water by distillation DMF- method, referred to as process water. 水法的缺点是工艺过程能耗高,热能消耗占DMF回收成本的80%以上,尤其不适用于含DMF浓度较低的稀废液处理。 Water Act disadvantage is the high energy consumption process, energy consumption accounts for more than 80% DMF recovery cost, in particular, does not apply to low concentrations of dilute DMF containing waste liquid treatment. 国内湿法移膜皮革生产过程中排放的废液内DMF往往浓度很低,如使用目前国内简单的DMF水法回收装置,由于能耗高,回收处理费用昂贵,使得工厂没有直接经济效益。 Domestic wet leather shift film production process emissions in DMF waste often very low concentration such as DMF using a simple domestic water recovery method, since high energy consumption, expensive recycling, such that the plant is no direct economic benefits. 如果将DMF废液直接排放到外界环境中,不仅是经济上的损失,而且造成严重的环境污染。 If the DMF discharged directly into the environment, not only economic loss, but also caused serious environmental pollution.

近十年来,我国PU革行业发展迅猛,生产竞争日趋激烈,节能和环保已经成为了一个不可忽视的问题,而且该行业大多集中在南方缺煤地区,年消耗标准煤数额巨大,如果能使单位能耗大幅下降,每年可产生的直接经济效益将十分可观。 Over the past decade, China's PU leather industry is growing, production increased competition, energy saving and environmental protection has become a problem can not be ignored, and most of the industry is concentrated in the southern coal shortage areas, the annual consumption of huge amounts of coal, if the unit can energy consumption dropped significantly, the direct economic benefits that can be generated per year will be very considerable.

发明内容 SUMMARY

本发明就是针对传统水法处理回收废水中DMF特别是低浓度DMF所具有的能耗大、经济效益低的缺点,提出的一种新的回收废水中DMF的方法。 The present invention is a new method for recycling waste of DMF was proposed for a conventional water recovery Wastewater Treatment DMF DMF particularly low concentration has a large power consumption, low economic disadvantage. 该方法首先通过溶剂萃取将废水中的DMF萃取到有机相中,然后通过精馏方法将有机溶剂与DMF分离,得到纯DMF产品。 Firstly wastewater DMF extracted by solvent extraction into the organic phase, then separated from the organic solvent by rectification method DMF, DMF to give the pure product.

本发明提供了一种废水中二甲基甲酰胺的回收方法,其特征在于:该方法主要包括萃取和精馏两个工序,首先采用有机溶剂萃取,将水溶液中的二甲基甲酰胺转移到有机溶剂中,然后再通过精馏实现二甲基甲酰胺与有机溶剂的分离。 The present invention provides a method for recovering wastewater dimethyl formamide, characterized in that: the method includes two distillation and extraction step, the organic solvent extraction is first employed to transfer aqueous solution of dimethylformamide to an organic solvent, then separation of dimethylformamide and the organic solvent by distillation.

进一步说,所述有机溶剂与二甲基甲酰胺的精馏分离工序分为初步分离和精制纯化两段,其中初步分离采用的精馏方式为常压精馏,而精制纯化采用的精馏方式为减压精馏。 Further, the organic solvent and distillation separation step dimethylformamide divided into two preliminary separation and purification purification, the manner in which the initial separation using distillation is atmospheric distillation, and purified by distillation in purification mode for the vacuum distillation.

在本发明中,所述有机溶剂与二甲基甲酰胺的精馏分离工序的精制纯化段采用侧线气相出料的方式采出二甲基甲酰胺。 In the present invention, the purified organic solvent and purification section of distillation separation step using dimethylformamide lateral line gas taken out of the material embodiment of dimethylformamide.

在所述精制纯化阶段向纯化塔中添加有机碱,以中和过程中产生的酸性物质,减少体系的腐蚀性。 Adding an organic base to the purification column in the purification purification stage, and an acidic substance generated in the process, reducing the corrosive system.

在本发明中,所述萃取工序设备可以采用填料萃取塔。 In the present invention, the extraction step extraction column packing apparatus may be employed.

本发明的有益效果是:1)整个分离回收过程能耗大大降低。 Advantageous effects of the present invention are: 1) the whole process of separating and recovering the energy consumption is greatly reduced. 本发明采用有机溶剂萃取技术将DMF与水的分离变为DMF与有机溶剂的分离。 The present invention uses an organic solvent extraction technique to separate DMF DMF and water becomes separated from the organic solvent. 萃取过程在常温下进行,能耗低,以处理规模1m3/hr为例,只需电耗0.75度/小时。 Extraction process at room temperature, low energy consumption, to process scale 1m3 / hr for example, the power consumption of only 0.75 degrees / hr. 所选有机萃取剂与水相比更易与DMF分离,有机萃取剂的蒸发潜热约为水的1/8,与DMF沸点差更大(大于等于80℃),分离过程需要的级数少,回流比低,蒸汽用量大大减少,能耗明显降低。 The organic extractant selected more easily than water is separated from the DMF, latent heat of evaporation of the organic extractant is about 1/8 of the water, the greater the difference between the boiling point of DMF (not less than 80 deg.] C), the separation process requires less number of stages, reflux ratio is low, greatly reduce steam consumption, energy consumption is significantly reduced. 以1m3/hr的废水(DMF 10%)处理规模为例,整个处理装置,只需1吨8公斤锅炉作为动力,使用负荷约为原来的60%;2)废水中的无机盐类、固形物是传统水法处理过程中必须考虑的问题,这些杂质容易在精馏工段蒸发器中析出、结垢,从而造成蒸发器列管的堵塞,难以清理,严重影响操作。 To 1m3 / hr wastewater (DMF 10%) Example process scale, the entire processing apparatus, only one t eight kg as a power boiler, using the original load is about 60%; 2) inorganic salts in the wastewater, solid must be considered is the problem of the conventional method of water treatment process, it tends to precipitate these impurities in the rectifying stage evaporator, fouling, thereby causing clogging of the evaporator tube, and difficult to clean, seriously affect the operation. 由于新方法采用有机溶剂萃取工艺,废水中的无机类杂质包括固形物都随水相排出,从而大大减少了传统工序中杂质进入精馏工序中而产生的精馏塔再沸器堵塞情况。 Since the new method with an organic solvent extraction process, wastewater impurities include inorganic solids are discharged with the water phase, thus greatly reducing the impurities into the conventional distillation step process generated congestion fractionator reboiler.

3)由于精馏工序分初步分离和精制纯化两段,其中精制纯化所采用的精馏方式为减压精馏,以降低分离过程的操作温度,使得整个回收过程温度不超过130℃,大大减少了DMF的分解和体系对分离设备材质的腐蚀作用,也提高了热利用率。 3) Since the distillation step of preliminary separation and purification purified fraction two, the manner in which rectification is purified purified using distillation under reduced pressure, to lower the operating temperature of the separation process, so that the entire recycling process temperature does not exceed 130 ℃, greatly reduced DMF and the decomposition system of the corrosive effects of the material separating apparatus, and also improve the thermal efficiency.

利用本发明所述方法回收的DMF的纯度可达到99.9%,回收率可达98.5%,相对于水法的经济性更好,因而可以处理低浓度的DMF废水,使得处理低于10%浓度的DMF废液也有利可图,在目前国际能源价格愈来愈高和环境保护日益重要的情况下,其应用前景十分广阔。 Using the method of the present invention may be recovered in a purity of 99.9% DMF, recovery rate of 98.5%, relative to the water approach is more economical, it is possible to process a low concentration of DMF wastewater, such treatment concentration less than 10% DMF waste is also profitable in the current international energy prices higher and higher and the growing importance of environmental protection, the application prospects.

附图说明 BRIEF DESCRIPTION

图1为本发明所述方法的一个实施例的流程框图。 A block flow diagram of FIG. 1 embodiment of the method of the present invention.

具体实施方式 detailed description

本发明提供了一种废水中二甲基甲酰胺(DMF)的回收方法,该方法主要包括萃取和精馏两个工序,首先采用有机溶剂萃取,将水溶液中的DMF转移到有机溶剂中,然后再通过精馏实现DMF与有机溶剂的分离。 The present invention provides a wastewater-dimethylformamide (DMF) is recovered, the method includes two distillation and extraction processes, first using an organic solvent, the aqueous solution will be transferred into the organic solvent in DMF, and then DMF and then separation of the organic solvent by distillation. 萃取剂选择满足以下性质的有机溶剂:1.与DMF有很好的相容性(一般为混溶);2.与水的相容性很低(在水中的溶解度<1%);3.与DMF的沸点差≥80℃。 Extractant selected organic solvent satisfies the following properties: 1 and have good compatibility DMF (usually miscible); 2 low compatibility with water (solubility of <1% in water); 3. and the boiling point of DMF difference ≥80 ℃. 常选的溶剂如氯仿、四氯化碳、1,1二氯乙烷、1,1,1三氯乙烷、1,2二氯乙烯、氯丙烷和三氯丙烯等。 Often choose a solvent such as chloroform, carbon tetrachloride, 1,1-dichloroethane, 1,1,1-trichloroethane, 1,2-dichloroethylene, trichloropropene chloropropane and the like. 所述有机溶剂与二甲基甲酰胺的精馏分离工序分为初步分离和精制纯化两段,其中初步分离采用的精馏方式为常压精馏,而精制纯化采用的精馏方式为减压精馏。 Distillation of the organic solvent dimethylformamide step into two preliminary separation and purification purification, the manner in which the initial separation using distillation is atmospheric distillation, and purified by distillation was purified by way of a reduced pressure distillation. 减压精溜的真空压力取值可在-0.04~-0.07MPa之间,真空度太小,起不到降低精溜塔内温度的效果,真空度太大则增大萃取剂损耗和真空能耗。 Vacuum pressure may be reduced fine slip values ​​between -0.04 ~ -0.07MPa, vacuum is too low, the effect of reducing not achieve fine slip column temperature, the degree of vacuum is too large, and the loss is increased to vacuum extraction agent consumption.

本发明具体实现如下:首先将低浓度DMF废水(质量百分比浓度≤10%)通入萃取塔,在萃取塔内废水与相应流比的有机溶剂进行液-液萃取传质交换,DMF由水相进入有机萃取相,废水中固形物等杂质则留在水相(萃余相)。 The present invention is embodied as follows: First, the low-concentration wastewater DMF (mass% concentration of ≤10%) into the extraction column, a liquid extraction column and the organic solvent waste stream corresponding ratio - mass transfer exchange liquid extraction, the aqueous phase DMF extracted into the organic phase, the wastewater solids and other impurities remain in the aqueous phase (raffinate phase). 然后含DMF的有机萃取相进入精馏分离工序。 The organic phase was extracted into the DMF-containing distillation separation step. 精馏分离工序分两段,即实现初步分离的浓缩塔和实现精制纯化的纯化塔。 Distillation separation step in two stages, i.e., to achieve preliminary separation and concentration to achieve purification column purification column purification. 浓缩塔为常压精馏塔,萃取相在其中浓缩成含DMF50%左右的有机溶液。 Concentrated under atmospheric pressure rectification column, in which the extract phase containing concentrated to about DMF50% of the organic solution. 最后将浓缩液通入DMF纯化塔,纯化塔为减压精馏塔,通过减压达到降低精馏温度,减少体系组分分解和腐蚀的目的。 Finally, the concentrate was purified by column into DMF and purified by vacuum distillation tower, distillation under reduced pressure to reduce the temperature, and the purpose of reducing corrosion of system components exploded. 纯度为99.9%的DMF通过侧线气相采出,冷凝后即可得到最终产品。 Purity of 99.9% in DMF side-by gas taken out, to obtain the final product is condensed.

本发明所述的回收工艺过程中产生的酸性杂质利用有机碱(如乙二胺、二乙胺等)进行反应中和,有机碱从纯化塔底部侧线连续按计量加入。 Acid impurities during the recovery process of the present invention is produced using an organic base (such as ethylenediamine, diethylamine, etc.), and the reaction, an organic base is added continuously metered from the bottom side of the line purification column. DMF水解的程度可以通过定期对体系精馏塔釜的酸碱度进行滴定来间接判断得到,并由此确定有机碱的加入量。 DMF hydrolysis degree of the system may periodically fractionator vessel titration by pH determination is obtained indirectly, and thereby determining the amount of an organic base.

因为本发明所述方法先通过低能耗萃取过程将DMF由水相转移至有机相,然后通过精馏将有机萃取剂与DMF分离,因此整个过程与传统水法相比能耗大大降低。 Because the method of the invention by first low-energy extraction process DMF transferred from the aqueous phase to the organic phase, then separated from the organic extractant with DMF by rectification, and therefore the whole process is greatly reduced energy consumption compared with conventional water method. 特别对于DMF浓度小于10%的废水,用传统水法回收时需要将90%以上的水蒸出,能耗巨大,从经济上变得不合理,而用本发明所述方法优势明显,可以取得经济和环境双效益。 Particularly less than 10% concentration of DMF for the waste water needs to be more than 90% of the water evaporated during recovery by conventional water method, enormous energy consumption, becomes economically unreasonable, but with the method of the present invention, significant advantages can be achieved economic and environmental double benefit.

下面结合附图来说明本发明的一个具体实施例。 Here will be described a specific embodiment of the present invention in conjunction with the accompanying drawings.

如图1所示,将10%(质量百分比浓度)的DMF水溶液以1.0吨/小时的流量进入填料萃取塔底部轻相入口,有机溶剂(氯仿)以2吨/小时的流量进入萃取塔顶部重相入口,有机相和水相在萃取塔中进行液-液萃取传质交换。 1, 10% (mass concentration) in DMF solution at 1.0 ton / hr of flow rate into the bottom of a light phase inlet packed extraction column, the organic solvent (chloroform) at 2 ton / hr of flow rate into the top of the extraction column weight inlet phase, an organic phase and an aqueous phase in the extraction column liquid - liquid extraction mass transfer exchange. 含DMF浓度为5%的有机萃取相由萃取塔重相出口通入浓缩塔。 Containing DMF concentration of 5% of the organic phase was extracted from the heavy phase outlet of the concentrating tower into the extraction column. 废水相从塔顶轻相出口流出,经萃取剂回收并进一步处理后排放。 Outlet to the waste water phase from overhead light, by recovering the extractant and further discharged after treatment. 浓缩塔为常压精馏,釜温为95℃,回流比为0.2。 Concentrated under atmospheric distillation tower, the pot temperature was 95 deg.] C, a reflux ratio of 0.2. 有机萃取相在浓缩塔中浓缩为DMF浓度约50%的有机溶液,由塔底排出。 The organic phase was extracted and concentrated to a DMF concentration of about 50% organic solution was concentrated in the column, it is discharged from the bottom. 浓缩塔顶馏出组分为萃取剂返回至萃取工序。 Concentrated overhead component extractant is returned to the extraction step. DMF浓度为50%的有机溶液从浓缩塔底部排出后进入纯化塔。 DMF concentration of 50% of the organic solution into the bottom of the purification column is discharged from the concentrating tower. 纯化塔为减压精馏塔,真空为-0.05MPa,塔釜温度为130℃。 Purified by vacuum distillation tower, a vacuum of -0.05 MPa, tower bottom temperature of 130 ℃.

有机溶液在该塔中通过减压精馏得到分离,塔顶为含有少量DMF(<1%)的有机萃取剂,返回浓缩塔入口。 The organic solution in the column was isolated by vacuum distillation overhead containing a small amount of an organic extractant DMF (<1%), the concentrating tower returns inlet. 纯度达99.9%的DMF以气相形式从侧线采出,经冷凝后得到最终产品。 DMF purity of 99.9% recovery in the form of vapor from the side of the line, condensed to give the final product.

回收工艺过程中产生的酸性杂质利用有机碱乙二胺进行反应中和,有机碱从纯化塔底部侧线连续按计量加入。 Acid impurities generated during the recovery process using an organic base in the reaction of ethylenediamine and the organic base are metered continuously from a bottom side of the line purification column. 体系中少量的固形物(废水中绝大部分固形物在萃取工艺中进入萃余项水相中,随水相排出)、废水中进入精馏系统的小分子树脂杂质受热产生的粘稠液及酸碱中和产物等定期从纯化塔底部排出。 A small amount of solids in the system (most of the solids in the wastewater entering the extraction process items aqueous raffinate phase, is discharged with the water phase), viscous liquid wastewater entering the distillation system a small molecule impurities heat generated and resin and periodic acid-base products, etc. withdrawn from the bottom of the purification column.

Claims (5)

  1. 1.一种废水中二甲基甲酰胺的回收方法,其特征在于:该方法主要包括萃取和精馏两个工序,首先采用有机溶剂萃取,将水溶液中的二甲基甲酰胺转移到有机溶剂中,然后再通过精馏实现二甲基甲酰胺与有机溶剂的分离。 1. A method for recovering wastewater dimethyl formamide, characterized in that: the method includes two distillation and extraction processes, first using an organic solvent, to transfer aqueous solution of dimethylformamide to an organic solvent , and then separation of dimethylformamide and the organic solvent by distillation.
  2. 2.根据权利要求1所述的废水中二甲基甲酰胺的回收方法,其特征在于:所述有机溶剂与二甲基甲酰胺的精馏分离工序分为初步分离和精制纯化两段,其中初步分离采用的精馏方式为常压精馏,而精制纯化采用的精馏方式为减压精馏。 The recovery method of claim 1 in wastewater dimethylformamide claim, wherein: said step of separating the organic solvent distillation of dimethylformamide is divided into two preliminary separation and purification of purified, wherein distillation primary separation mode used is atmospheric distillation, and purified by distillation was purified by way of reduced pressure distillation.
  3. 3.根据权利要求1所述的废水中二甲基甲酰胺的回收方法,其特征在于:所述有机溶剂与二甲基甲酰胺的精馏分离工序的精制纯化段采用侧线气相出料的方式采出二甲基甲酰胺。 The recovery method of claim 1 in wastewater dimethylformamide claim, wherein: refined purification section distillation separation step of the organic solvent and dimethyl formamide by way of the discharge-side gas line Produced dimethylformamide.
  4. 4.根据权利要求1所述的废水中二甲基甲酰胺的回收方法,其特征在于:在所述精制纯化阶段向纯化塔中添加有机碱,以中和过程中产生的酸性物质,减少体系的腐蚀性。 The wastewater recovery method of claim 1 dimethylformamide claim, characterized in that: adding an organic base to the purification column in the purification stage refining, to neutralize acidic substance generated in the process, reducing system corrosive.
  5. 5.根据权利要求1所述的废水中二甲基甲酰胺的回收方法,其特征在于:所述萃取工序设备采用填料萃取塔。 The recovery method of claim 1 in wastewater dimethylformamide claim, wherein: the extraction step using the apparatus packed extraction column.
CN 200510086784 2005-11-04 2005-11-04 Process for recovering dimethyl formyl amide from waste water CN1317259C (en)

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100551903C (en) 2007-01-11 2009-10-21 清华大学 Process for recovering dimethyl amide from waste water using ion liquid extracting process
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 Process for treating DMF (Dimethyl Formamide) wastewater through distillation by using low-pressure double-effect dual-heat pump

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100551903C (en) 2007-01-11 2009-10-21 清华大学 Process for recovering dimethyl amide from waste water using ion liquid extracting 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
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 method for separating high and low pressure distillation towers 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 Process for treating DMF (Dimethyl Formamide) wastewater through distillation by using low-pressure double-effect dual-heat pump

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