CN103333080A - 含dmf废水四效精馏回收方法 - Google Patents
含dmf废水四效精馏回收方法 Download PDFInfo
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- CN103333080A CN103333080A CN201310304564XA CN201310304564A CN103333080A CN 103333080 A CN103333080 A CN 103333080A CN 201310304564X A CN201310304564X A CN 201310304564XA CN 201310304564 A CN201310304564 A CN 201310304564A CN 103333080 A CN103333080 A CN 103333080A
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- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-dimethylformamide Chemical compound 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Abstract
本发明公开了一种含DMF废水四效精馏回收方法,包括脱胺塔热量利用、一级减压精馏塔出料大循环技术、常压精馏塔气相出料至脱酸塔以及脱酸塔上下回流等技术的改进和创新方法。本发明使系统内部热能充分利用,既降低了冷媒循环水的循环量,又节省了一次热源的消耗量,且使整个系统的操作运行更稳定、简单,DMF的成品品质更易控制。本工艺技术改进方法同样可应用到三效DMF回收系统中。
Description
含DMF废水四效精馏回收方法
技术领域
[0001 ] 本发明涉及一种溶剂回收方法,具体是涉及一种含DMF废水四效精馏回收方法,属于DMF的分离纯化领域。
背景技术
[0002] DMF又名N,N- 二甲基甲酰胺。作为一种强极性溶剂,是重要的有机化工原料和优良的溶剂,在医药工业中用于制造抗菌素、激素等药物,化纤工业用于聚丙烯腈纺丝,农药工业用于制造高效低毒农药杀虫脒,石化工业用作气体吸收剂和乙炔溶剂,有机工业用作合成有机化合物的原料,塑料工业用作乙烯树脂的溶剂,分析化学中用作非水滴定的溶剂、气相色谱固存定液、分离分析C2 — C3烃类、正异丁烯-1及顺-反丁烯_2,同时大量用于合成革的制造,染料、绝缘材料的生产。目前超纤、手套、湿法合成革行业应用量非常大,每年产生的废水超过600万吨。
[0003] DMF受热易分解为甲酸和二甲胺,甲酸和二甲胺的存在会严重影响DMF的产品质量,其含量是判定DMF质量好坏的重要标准。
[0004] 目前已经有DMF的四效精馏回收工艺,如专利号为200910228354.0的中国专利公开了一种湿法合成革二甲基甲酰胺溶液四效精馏系统及回收方法,虽然在节能效果上有很大改进,但仍有部分热量没有被充分利用,并且由于四效回收系统加热流程加长,DMF的分解量也有所增加,这就对脱酸塔脱酸方式有一定的要求,且对操作人员的操作能力要求很高,DMF成品品质难控制。
发明内容
[0005] 本发明的目的是提供一种含DMF废水四效精馏回收方法,以解决现有的DMF四效工艺仍有部分热量不能被充分利用、系统难操作、成品品质难控制等缺点。
[0006] 本发明采用的技术方案:
一种含DMF废水四效精馏回收方法,包括如下内容:含DMF的废水经废水预热器预热后依次经过一级减压精馏塔、二级减压精馏塔、三级减压精馏塔、常压精馏塔和脱酸塔后出料,二级减压精馏塔的塔顶蒸汽经再沸器预热一级减压精馏塔的物料,三级减压精馏塔的塔顶蒸汽经再沸器预热二级减压精馏塔的物料,常压精馏塔的塔顶蒸汽经再沸器预热三级减压精馏塔的物料,脱酸塔的塔顶蒸汽经过大回流预热器全部回流至脱酸塔上部,一级减压精馏塔的塔釜出料经大回流预热器预热后按分流比6:1分别进一级减压精馏塔和二级减压精馏塔。
[0007] 作为本发明的进一步改进,各精馏塔的塔顶水经塔顶水预热器进入脱胺塔以脱去其中的二甲胺,脱胺塔内脱去二甲胺后的塔釜液依次经塔顶水预热器和废液预热器,预热塔顶水和含DMF的废水后回用至生产线,脱胺塔的塔顶蒸汽经再沸器预热二级减压精馏塔的物料。
[0008] 作为本发明的进一步改进,脱酸塔出料按分流比2:1分别作为成品出料和回流至脱酸塔。
[0009] 作为本发明的进一步改进,常压精馏塔出料由第5块理论板以下位置气相出料至脱酸塔塔釜的气相空间,脱酸塔塔釜累积液体经返液罐和返液泵送至常压精馏塔塔釜。
[0010] 采用上述技术方案的有益效果在于:
(I)本发明使用一级减压精馏塔塔釜液体大循环工艺,利用一级减压精馏塔塔釜液体(54-56°C)冷凝脱酸塔塔顶蒸汽(95-100°C)。经泵压缩后塔釜液体沸点上升,与DMF蒸汽换热后按照6:1的比例分流,大部分过热液体返回一级浓缩塔闪蒸,另一部分出料至二级减压精馏塔维持二级浓缩塔液位。现有DMF四效工艺中脱酸塔塔顶蒸汽只用于废液进料的预热,因进料流量一定,所以被利用的热量是有限的,大部分热量是靠循环水带走的。本工艺改进技术采用一级减压精馏塔塔釜液大循环把脱酸塔塔顶潜热热量全部带走,脱酸塔塔顶蒸汽冷凝的热量全部传递到一级浓缩塔,节约了大量能源。
[0011] (2)本发明将脱胺塔塔顶、塔釜的热量均做了充分利用。脱胺塔塔釜液(100-102 °C )预热未经脱胺处理的塔顶水(70-75 °C )后再来预热DMF废液进料(25 °C );脱胺塔塔顶蒸汽(IOO0C )经再沸器加热二级减压精馏塔(68-69°C )。通过进出物料温度的差,用冷物料冷却热物料,不仅吸收高温物料的热量同时减少了冷媒循环水的使用量。
[0012] (3)本发明脱酸塔采用上下回流方式。上回流为塔顶蒸汽通过大回流预热器全回流,主要脱除产品中水分及轻组分,下回流采用侧线出料口以下位置回流,下回流采用成品回流,由于回流液温度低,更有利于脱酸塔中高沸点的甲酸DMF气相混合物冷凝,可以在减少回流比的情况下达到脱酸效果,采用脱酸塔上下回流的方式,不但使脱酸塔的操控更容易,DMF的成品品质更稳定,纯度达到99.99%,水含量低于lOOppm,酸度低于lOppm,碱度低于5ppm,并且还有效的降低了能耗,一举两得。
[0013] (4)本发明采用精馏塔气相出料至脱酸塔的工艺,由精馏塔塔釜第5块理论板以下位置气相出料至脱酸塔塔釜 气相空间,脱酸塔塔釜累积液体经返液泵送至精馏塔塔釜。由于在同等温度下,甲酸的分解速率是DMF的6倍,因此返液泵打至精馏塔塔釜的高酸液体酸值会下降,与精馏塔提馏段下降的液体混合后,综合酸值低于脱酸塔塔釜酸值,相对于脱酸塔来说,塔釜与塔顶甲酸浓度差减小,有利于脱酸塔的稳定操作,同时可以大幅减少塔釜高酸混合液的抽出量,提高产品回收率至99%。
[0014] 本发明使系统内部热能充分利用,既降低了冷媒循环水的循环量,又节省了一次热源的消耗量,且使整个系统的操作运行更稳定、简单,DMF的成品品质更易控制。本工艺技术改进方法同样可应用到三效DMF回收系统中。
附图说明
[0015] 图1为本发明DMF四效回收工艺原理图;
图2为现有DMF四效回收工艺原理图。
具体实施方式
[0016] 如图1所示,本发明含DMF废水四效精馏回收方法包括:含DMF的废水经废水预热器预热后依次经过一级减压精馏塔(塔顶压力为9-12Kpa,塔底温度为54-56°C)、二级减压精馏塔(塔顶压力为23-27Kpa,塔底温度为68-69°C )、三级减压精馏塔(塔顶压力为44-49Kpa,塔底温度为85-89 °C )、常压精馏塔(100-103°C )和脱酸塔后出料,二级减压精馏塔的塔顶蒸汽经再沸器预热一级减压精馏塔的物料,三级减压精馏塔的塔顶蒸汽经再沸器预热二级减压精馏塔的物料,常压精馏塔的塔顶蒸汽经再沸器预热三级减压精馏塔的物料,脱酸塔的塔顶蒸汽经过大回流预热器全部回流至脱酸塔上部,一级减压精馏塔的塔釜出料经大回流预热器预热后按分流比6:1分别进一级减压精馏塔和二级减压精馏塔。
[0017] 各精馏塔的塔顶出料为水和微量低沸点的二甲胺,经塔顶水预热器进入脱胺塔以脱去其中的二甲胺,脱胺塔内脱去二甲胺后的塔釜液依次经塔顶水预热器和废液预热器,预热塔顶水和含DMF的废液原料后回用至生产线,脱胺塔的塔顶蒸汽经再沸器预热二级减压精馏塔的物料,被物料冷却后进入锅炉焚烧。
[0018] 脱酸塔出料按分流比2:1分别作为成品出料和回流至脱酸塔。
[0019] 常压精馏塔出料由第5块理论板以下位置气相出料至脱酸塔塔釜的气相空间,脱酸塔塔釜累积液体经返液罐和返液泵送至常压精馏塔塔釜。
[0020] 如图2所示,现有DMF四效回收工艺包括:DMF废液进料经脱酸塔塔顶蒸汽预热、三级脱水、精馏、脱酸、脱胺出料等构成。脱胺塔塔顶蒸汽及塔釜出水目前采用直接水冷的方式,既使这部分热量浪费了,又需要大量循环水把热量带走;脱酸塔塔顶蒸汽预热废液进料,由于进料量一定,废液带走的热量有限,大部分热量需要到下一级用循环水带走;精馏塔采用塔釜液相出料至脱酸塔,会把重组分和甲酸带入脱酸塔中,对脱酸塔的操作要求较高;脱酸塔只用上回流,侧线采出的DMF中酸值不易控制,需要操作人员对出料品质做频繁的检测,增加操作人员的工作量也对操作人员的操作水平要求较高。
[0021] 本发明和图2所示现有工艺的能耗对照如表I所示。
[0022] 表I本发明和现有DMF四效回收工艺的能耗对照表
由上表可见,本发明工艺与现有的DMF四效回收工艺相比具有明显的优势,适合在工业生产中应用。本领域技术人员在本发明基础上所做的基础的改进,如减少一个减压精馏塔的数量进行DMF的三效回收,亦在本发明的保护范围之内。
Claims (4)
1.一种含DMF废水四效精馏回收方法,其特征在于:含DMF的废水经废水预热器预热后依次经过一级减压精馏塔、二级减压精馏塔、三级减压精馏塔、常压精馏塔和脱酸塔后出料;二级减压精馏塔的塔顶蒸汽经再沸器预热一级减压精馏塔的物料,三级减压精馏塔的塔顶蒸汽经再沸器预热二级减压精馏塔的物料,常压精馏塔的塔顶蒸汽经再沸器预热三级减压精馏塔的物料,脱酸塔的塔顶蒸汽经过大回流预热器冷却后全部回流至脱酸塔上部,一级减压精馏塔的塔釜出料经大回流预热器预热后按分流比6:1分别进一级减压精馏塔和二级减压精馏塔。
2.根据权利要求1所述的方法,其特征在于各精馏塔的塔顶水经塔顶水预热器进入脱胺塔以脱去其中的二甲胺,脱胺塔内脱去二甲胺后的塔釜液依次经塔顶水预热器和废液预热器,预热塔顶水和含DMF的废水后回用至生产线,脱胺塔的塔顶蒸汽经再沸器预热二级减压精馏塔的物料。
3.根据权利要求2所述的方法,其特征在于脱酸塔出料按分流比2:1分别作为成品出料和回流至脱酸塔。
4.根据权利要求3所述的方法,其特征在于常压精馏塔出料由第5块理论板以下位置气相出料至脱酸塔塔釜的气相空间,脱酸塔塔釜累积液体经返液罐和返液泵送至常压精馏
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CN108218756A (zh) * | 2018-03-08 | 2018-06-29 | 梁沛文 | 一种nmp废水低温回收系统及其方法 |
CN110937744A (zh) * | 2019-12-09 | 2020-03-31 | 西安交通大学 | 一种合成革dmf废水热泵精馏过程中的二甲胺处理工艺 |
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