CN221117061U - MVR coupling multi-effect rectification imidacloprid wastewater recycling device - Google Patents
MVR coupling multi-effect rectification imidacloprid wastewater recycling device Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 35
- 239000005906 Imidacloprid Substances 0.000 title claims abstract description 21
- YWTYJOPNNQFBPC-UHFFFAOYSA-N imidacloprid Chemical compound [O-][N+](=O)\N=C1/NCCN1CC1=CC=C(Cl)N=C1 YWTYJOPNNQFBPC-UHFFFAOYSA-N 0.000 title claims abstract description 21
- 229940056881 imidacloprid Drugs 0.000 title claims abstract description 21
- 238000004064 recycling Methods 0.000 title description 16
- 230000008878 coupling Effects 0.000 title description 3
- 238000010168 coupling process Methods 0.000 title description 3
- 238000005859 coupling reaction Methods 0.000 title description 3
- 238000004821 distillation Methods 0.000 claims abstract description 135
- 239000007788 liquid Substances 0.000 claims abstract description 112
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 103
- 238000011084 recovery Methods 0.000 claims abstract description 61
- 239000012153 distilled water Substances 0.000 claims abstract description 60
- 239000011552 falling film Substances 0.000 claims abstract description 46
- 238000004519 manufacturing process Methods 0.000 claims abstract description 38
- 238000000605 extraction Methods 0.000 claims abstract description 27
- WRYCSMQKUKOKBP-UHFFFAOYSA-N Imidazolidine Chemical compound C1CNCN1 WRYCSMQKUKOKBP-UHFFFAOYSA-N 0.000 claims description 25
- 238000000926 separation method Methods 0.000 claims description 23
- 238000010438 heat treatment Methods 0.000 claims description 22
- 239000012141 concentrate Substances 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 10
- 238000010992 reflux Methods 0.000 claims description 10
- 239000002994 raw material Substances 0.000 claims description 8
- 239000002912 waste gas Substances 0.000 claims description 5
- 238000012545 processing Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 22
- 239000000575 pesticide Substances 0.000 abstract description 15
- 238000013461 design Methods 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 238000012546 transfer Methods 0.000 abstract description 8
- 229910052799 carbon Inorganic materials 0.000 abstract description 3
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-dimethylformamide Substances CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 24
- 238000005406 washing Methods 0.000 description 14
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 238000001816 cooling Methods 0.000 description 6
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 5
- 239000012452 mother liquor Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 4
- RAXXELZNTBOGNW-UHFFFAOYSA-N imidazole Natural products C1=CNC=N1 RAXXELZNTBOGNW-UHFFFAOYSA-N 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 101001121408 Homo sapiens L-amino-acid oxidase Proteins 0.000 description 2
- 102100026388 L-amino-acid oxidase Human genes 0.000 description 2
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- 238000007906 compression Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
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- MTNDZQHUAFNZQY-UHFFFAOYSA-N imidazoline Chemical compound C1CN=CN1 MTNDZQHUAFNZQY-UHFFFAOYSA-N 0.000 description 2
- 238000011197 physicochemical method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 101100012902 Saccharomyces cerevisiae (strain ATCC 204508 / S288c) FIG2 gene Proteins 0.000 description 1
- 101100233916 Saccharomyces cerevisiae (strain ATCC 204508 / S288c) KAR5 gene Proteins 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
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- 231100000086 high toxicity Toxicity 0.000 description 1
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- 238000005457 optimization Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
本实用新型公开了一种MVR耦合多效精馏吡虫啉废水资源化回收装置，包括脱轻塔、脱重塔、精馏塔、MVR压缩机、MVR降膜再沸器、MVR蒸馏水罐、原液箱、二级原液加热器、原液泵、脱轻冷凝器、脱轻罐、脱轻再沸器、脱轻循环泵、脱轻料液泵和脱轻采出泵。本装置结合三维变空间顺紊流设计方法对多效精馏系统的能量传递设备或装置进行优化设计，可以缩小能量传递设备的换热端差，降低能量传递系统动力消耗，进一步降低多效精馏系统的能量消耗，实现多效精馏农药生产废水资源化回收系统的低碳运行。
The utility model discloses an MVR coupled multi-effect distillation imidacloprid wastewater resource recovery device, including a light removal tower, a heavy removal tower, a distillation tower, an MVR compressor, an MVR falling film reboiler, an MVR distilled water tank, a stock liquid tank, a secondary stock liquid heater, a stock liquid pump, a light removal condenser, a light removal tank, a light removal reboiler, a light removal circulation pump, a light removal liquid pump and a light removal extraction pump. The device optimizes the design of the energy transfer equipment or device of the multi-effect distillation system by combining the three-dimensional variable space turbulent flow design method, which can reduce the heat transfer end difference of the energy transfer equipment, reduce the power consumption of the energy transfer system, further reduce the energy consumption of the multi-effect distillation system, and realize the low-carbon operation of the multi-effect distillation pesticide production wastewater resource recovery system.
Description
技术领域Technical Field
本实用新型涉及农药生产废水资源化回收设备技术领域，尤其涉及一种MVR耦合多效精馏吡虫啉废水资源化回收装置。The utility model relates to the technical field of pesticide production wastewater resource recovery equipment, in particular to an MVR coupled multi-effect distillation imidacloprid wastewater resource recovery device.
背景技术Background technique
我国是世界农药生产大国，农药工业的污染主要来自于生产过程中所排放的废水，2020年，全国农药工业每年排放废水约2.5亿吨，主要涉及生产过程中的排水、产品洗涤水、设备和车间地面的清洗水等。农药生产废水历来以毒性大、浓度高、治理难成为社会关注的重点。农药生产废水处理技术根据采用原理的不同可分为物化法、化学法、生化法和焚烧法。萃取和精馏是处理农药生产废水最广泛的物化法，由于萃取需要使用溶剂，结合精馏方式对溶剂进行回收，是避免溶剂二次污染的有效方式，也便于实现农药生产废水的资源化回用。但精馏法耗能大，处理成本高。现有多效蒸馏设备结构复杂，工艺流程长，资源利用率不高，设备和人工成本高。my country is a major pesticide producer in the world. The pollution of the pesticide industry mainly comes from the wastewater discharged during the production process. In 2020, the national pesticide industry discharged about 250 million tons of wastewater each year, mainly involving drainage in the production process, product washing water, equipment and workshop floor cleaning water, etc. Pesticide production wastewater has always been the focus of social attention due to its high toxicity, high concentration and difficulty in treatment. Pesticide production wastewater treatment technology can be divided into physicochemical method, chemical method, biochemical method and incineration method according to different principles. Extraction and distillation are the most widely used physicochemical methods for treating pesticide production wastewater. Since extraction requires the use of solvents, combining distillation to recover solvents is an effective way to avoid secondary pollution of solvents, and it is also convenient to realize the resource reuse of pesticide production wastewater. However, the distillation method consumes a lot of energy and has high treatment costs. The existing multi-effect distillation equipment has a complex structure, a long process flow, low resource utilization, and high equipment and labor costs.
实用新型内容Utility Model Content
本实用新型的目的是克服上述现有技术的不足，提供一种MVR耦合多效精馏吡虫啉废水资源化回收装置。The utility model aims to overcome the deficiencies of the prior art and provide an MVR coupled multi-effect distillation imidacloprid wastewater resource recovery device.
本实用新型是通过以下技术方案来实现的：一种MVR耦合多效精馏吡虫啉废水资源化回收装置，装置包括原液箱、二级原液加热器、原液泵、脱轻冷凝器、脱轻罐、脱轻再沸器、脱轻循环泵、脱轻料液泵和脱轻采出泵；所述脱轻塔前设置有所述原液箱和所述二级原液加热器，所述二级原液加热器的热源分别来自回收的MVR蒸馏水和所述脱轻塔及所述精馏塔的冷凝水显热；所述二级原液加热器包括蒸馏水原液加热器和与其相连的冷凝水原液加热器；所述原液箱进口与来自生产车间的原料液通过连接管道连接，所述原液泵的入口与所述原液箱相连，所述原液泵的出口与所述蒸馏水原液加热器相连；所述脱轻塔塔顶与所述脱轻冷凝器、所述脱轻罐分别连接，所述脱轻塔底部通过所述脱轻循环泵与所述脱轻再沸器底部管程相连，所述脱轻再沸器上部管程与所述脱轻塔下部相连；所述脱轻冷凝器与所述脱轻罐还连接有用于抽出所述脱轻塔内不凝气体的脱轻真空泵；所述脱轻罐底部通过所述脱轻采出泵与厂区回收系统连接；所述脱轻塔底部通过所述脱轻料液泵与所述脱重塔相连；所述脱轻再沸器的热源来自厂区供热蒸汽，所述脱轻再沸器通过第二冷凝水回收接口与所述冷凝水原液加热器连接，加热蒸汽走壳程，释放潜热后通过第二冷凝水回收接口与冷凝水原液加热器连接，并在冷凝水原液加热器内进一步释放显热后回收利用。从脱轻塔塔顶蒸出的轻组份在脱轻冷凝器冷凝，一部分回流到脱轻塔，另一部分进入脱轻罐后回收；脱轻塔塔底有脱轻再沸器，热源来自厂区供热蒸汽，加热蒸汽走壳程，释放潜热后经第二冷凝水回收接口送至冷凝水原液加热器，进一步释放显热后回到厂区凝水收集系统；脱轻塔底设有出料泵(脱轻料液泵)采出含有DMF和咪唑烷的热水至脱重塔。The utility model is realized through the following technical scheme: an MVR coupled multi-effect distillation imidacloprid wastewater resource recovery device, the device comprises a stock liquid tank, a secondary stock liquid heater, a stock liquid pump, a light removal condenser, a light removal tank, a light removal reboiler, a light removal circulation pump, a light removal liquid pump and a light removal extraction pump; the stock liquid tank and the secondary stock liquid heater are arranged in front of the light removal tower, and the heat sources of the secondary stock liquid heater come from the recovered MVR distilled water and the sensible heat of the condensed water of the light removal tower and the distillation tower respectively; the secondary stock liquid heater comprises a distilled water stock liquid heater and a condensed water stock liquid heater connected thereto; the stock liquid tank inlet is connected to the raw material liquid from the production workshop through a connecting pipe, the stock liquid pump inlet is connected to the stock liquid tank, and the stock liquid pump outlet is connected to the distilled water stock liquid heater; the light removal tower The top is connected to the de-lightness condenser and the de-lightness tank respectively, the bottom of the de-lightness tower is connected to the bottom pipe side of the de-lightness reboiler through the de-lightness circulation pump, and the upper pipe side of the de-lightness reboiler is connected to the lower part of the de-lightness tower; the de-lightness condenser and the de-lightness tank are also connected with a de-lightness vacuum pump for extracting non-condensable gas in the de-lightness tower; the bottom of the de-lightness tank is connected to the plant recovery system through the de-lightness extraction pump; the bottom of the de-lightness tower is connected to the de-heavy tower through the de-lightness liquid pump; the heat source of the de-lightness reboiler comes from the plant heating steam, the de-lightness reboiler is connected to the condensate stock liquid heater through the second condensate recovery interface, the heating steam goes through the shell side, and after releasing the latent heat, it is connected to the condensate stock liquid heater through the second condensate recovery interface, and is recycled after further releasing the sensible heat in the condensate stock liquid heater. The light components evaporated from the top of the light-removal tower are condensed in the light-removal condenser, with a part of it refluxed to the light-removal tower and the other part entering the light-removal tank for recovery; there is a light-removal reboiler at the bottom of the light-removal tower, and the heat source comes from the heating steam in the plant area. The heating steam goes through the shell side, and after releasing the latent heat, it is sent to the condensate raw liquid heater through the second condensate recovery interface, and after further releasing the sensible heat, it returns to the condensate collection system in the plant area; a discharge pump (light-removal liquid pump) is provided at the bottom of the light-removal tower to extract hot water containing DMF and imidazolidine to the heavy-removal tower.
装置还包括降膜循环泵、脱重料液泵、蒸馏水回流泵、蒸馏水回收泵和第一冷凝水回收接口；所述脱重塔顶部与所述MVR压缩机连接，所述MVR压缩机与所述MVR降膜再沸器上部壳程连接；所述MVR降膜再沸器底部管程与所述脱重塔下部连接，所述MVR降膜再沸器管程顶部通过所述降膜循环泵与所述脱重塔底部连接；所述MVR降膜再沸器壳程底部与所述MVR蒸馏水罐相连，所述MVR蒸馏水罐出口依次通过所述蒸馏水回收泵、所述第一冷凝水回收接口与所述蒸馏水原液加热器连接，所述MVR蒸馏水罐出口还通过所述蒸馏水回流泵与所述脱重塔上部连接；所述脱重塔底部通过所述脱重料液泵与所述精馏塔连接。脱重塔塔顶蒸汽先进入MVR压缩机，增焓升温后进入塔底MVR降膜再沸器壳侧，释放潜热后再进入MVR蒸馏水罐；脱重塔塔底设有降膜循环泵，将物料泵入MVR降膜再沸器，在加热器管内降膜加热后回流至脱重塔；MVR蒸馏水罐收集MVR降膜再沸器的冷凝水，一部分回流至脱重塔塔顶，另一部分泵送至蒸馏水原液加热器，进一步释放显热后回生产水洗岗位循环套用；脱重塔塔底还设有脱重料液泵，将富含有咪唑烷和DMF的母液泵至精馏塔。The device also includes a falling film circulation pump, a deweighting liquid pump, a distilled water reflux pump, a distilled water recovery pump and a first condensed water recovery interface; the top of the deweighting tower is connected to the MVR compressor, and the MVR compressor is connected to the upper shell side of the MVR falling film reboiler; the bottom tube side of the MVR falling film reboiler is connected to the lower part of the deweighting tower, and the top of the MVR falling film reboiler tube side is connected to the bottom of the deweighting tower through the falling film circulation pump; the bottom of the MVR falling film reboiler shell side is connected to the MVR distilled water tank, and the outlet of the MVR distilled water tank is connected to the distilled water stock liquid heater through the distilled water recovery pump and the first condensed water recovery interface in sequence, and the outlet of the MVR distilled water tank is also connected to the upper part of the deweighting tower through the distilled water reflux pump; the bottom of the deweighting tower is connected to the distillation tower through the deweighting liquid pump. The steam from the top of the de-weighting tower first enters the MVR compressor, and after increasing enthalpy and rising in temperature, it enters the shell side of the MVR falling film reboiler at the bottom of the tower, and then enters the MVR distilled water tank after releasing latent heat; a falling film circulation pump is provided at the bottom of the de-weighting tower to pump the material into the MVR falling film reboiler, and after falling film heating in the heater tube, it flows back to the de-weighting tower; the MVR distilled water tank collects the condensed water from the MVR falling film reboiler, part of which flows back to the top of the de-weighting tower, and the other part is pumped to the distilled water stock liquid heater, and after further releasing sensible heat, it returns to the production water washing station for circulation; a de-weighting liquid pump is also provided at the bottom of the de-weighting tower to pump the mother liquor rich in imidazolidine and DMF to the distillation tower.
装置还包括精馏冷凝器、提浓分离罐、精馏再沸器、DMF浓液采出泵、咪唑烷浓液采出泵、强制循环泵和蒸馏真空泵；所述精馏塔顶部出口与所述精馏冷凝器连接，所述提浓分离罐与所述精馏塔上部进口连接，所述精馏冷凝器的一出口通过连接管连接在所述提浓分离罐与所述精馏塔之间的连接管路上；所述提浓分离罐与所述精馏冷凝器并接在所述蒸馏真空泵上，并通过所述蒸馏真空泵与车间废气处理系统连接；所述提浓分离罐底部通过所述富含DMF的DMF浓液采出泵与厂区回收系统连接；所述精馏塔底部通过所述强制循环泵与所述精馏再沸器底部管程连接，所述精馏再沸器管程顶部与所述精馏塔下部连接，所述精馏再沸器下部壳程通过第二冷凝水回收接口与所述冷凝水原液加热器连接，所述精馏再沸器的热源来自厂区供热蒸汽并进入精馏再沸器壳程；所述精馏塔底部通过所述咪唑烷浓液采出泵送回生产线套用。从精馏塔塔顶精馏冷凝器冷凝出的富含DMF的冷凝液，一部分回流到精馏塔，另一部分进入提浓分离罐后回收再利用；精馏塔塔底有精馏再沸器，热源来自厂区供热蒸汽，第二冷凝水回收接口送至冷凝水原液加热器，释放显热后回到厂区凝水收集系统；精馏塔底设有出料泵(咪唑烷浓液采出泵)采出富含咪唑烷的浓液泵送至回生产线套用。The device also includes a distillation condenser, a concentration separation tank, a distillation reboiler, a DMF concentrate extraction pump, an imidazolidine concentrate extraction pump, a forced circulation pump and a distillation vacuum pump; the top outlet of the distillation tower is connected to the distillation condenser, the concentration separation tank is connected to the upper inlet of the distillation tower, and an outlet of the distillation condenser is connected to the connecting pipeline between the concentration separation tank and the distillation tower through a connecting pipe; the concentration separation tank and the distillation condenser are connected to the distillation vacuum pump in parallel, and are connected to the workshop waste gas treatment system through the distillation vacuum pump. The bottom of the concentration and separation tank is connected to the plant recovery system through the DMF-rich DMF concentrate extraction pump; the bottom of the distillation tower is connected to the bottom pipe side of the distillation reboiler through the forced circulation pump, the top of the distillation reboiler pipe side is connected to the lower part of the distillation tower, the lower shell side of the distillation reboiler is connected to the condensate stock heater through the second condensate recovery interface, the heat source of the distillation reboiler comes from the plant heating steam and enters the distillation reboiler shell side; the bottom of the distillation tower is sent back to the production line for application through the imidazolidine concentrate extraction pump. A part of the DMF-rich condensate condensed from the distillation condenser at the top of the distillation tower is refluxed to the distillation tower, and the other part enters the concentration separation tank for recycling and reuse; there is a distillation reboiler at the bottom of the distillation tower, and the heat source comes from the heating steam of the plant area. The second condensate recovery interface is sent to the condensate raw liquid heater, and returns to the condensate collection system of the plant area after releasing the sensible heat; a discharge pump (imidazole concentrate extraction pump) is provided at the bottom of the distillation tower to extract the imidazolidine-rich concentrate and pump it back to the production line for application.
所述MVR降膜再沸器采用扭曲椭圆管作为加热器换热管束，所述MVR降膜再沸器的筒体内设置有用于包裹换热管束的导流筒。The MVR falling film reboiler adopts twisted elliptical tubes as the heater heat exchange tube bundle, and a guide tube for wrapping the heat exchange tube bundle is arranged in the cylinder of the MVR falling film reboiler.
所述脱轻再沸器和精馏再沸器均采用扭曲椭圆管并行设置的换热管束；所述蒸馏水原液加热器和冷凝水原液加热器采用扭曲椭圆管管壳式换热器或板式换热器。The light removal reboiler and the rectification reboiler both use heat exchange tube bundles with twisted elliptical tubes arranged in parallel; the distilled water stock heater and the condensed water stock heater use twisted elliptical tube shell and tube heat exchangers or plate heat exchangers.
所述脱轻塔与所述脱重塔均采用板式塔结构，所述精馏塔采用板式塔结构或填料塔结构。The light-removal tower and the heavy-removal tower both adopt a plate tower structure, and the distillation tower adopts a plate tower structure or a packed tower structure.
管壳式加热器与再沸器的换热管束由若干高比表面的扭曲椭圆管通过捆扎并使得管束间形成凸点接触而构成相互支撑结构，形成轴向多通道的流通通道，无需设折流板或中间支撑管板；扭曲椭圆管的横截面为近椭圆形，经过二次加工扭曲形成螺旋状结构。换热管束之间形成轴向多通道的三维变空间顺紊流设计，可缩小换热端差，降低能量损耗，提高热交换效率。The heat exchange tube bundles of the shell and tube heater and the reboiler are composed of several twisted elliptical tubes with high specific surface area, which are bundled and form convex contact between the tube bundles to form a mutual support structure, forming an axial multi-channel flow channel without the need for baffles or intermediate support tube sheets; the cross section of the twisted elliptical tube is nearly elliptical, and after secondary processing, it is twisted to form a spiral structure. The three-dimensional variable space turbulent flow design with axial multi-channels between the heat exchange tube bundles can reduce the heat exchange end difference, reduce energy loss, and improve heat exchange efficiency.
与现有技术对比，本实用新型的优点在于：本装置利用回收脱重塔采出蒸汽潜热为脱重再沸器热源，由于脱重塔的用热占整个多效精馏系统的80％以上，通过MVR装置对脱重塔采出蒸汽进行增焓升温，用于塔底再沸加热，可以大大降低脱重塔的能量消耗，避免了采用塔顶冷凝器冷却回收蒸馏水，因而也降低了冷却系统的能耗和水耗，实现农药生产废水资源化回收过程的节能节水。结合三维变空间顺紊流设计方法对多效精馏系统的能量传递设备或装置进行优化设计，可以缩小能量传递设备的换热端差，降低能量传递系统动力消耗，进一步降低多效精馏系统的能量消耗，实现多效精馏农药生产废水资源化回收系统的低碳运行。无折流板的相互支撑结构的再沸器运行可靠性和换热性能得到明显提升。Compared with the prior art, the advantages of the utility model are: the device utilizes the latent heat of the steam produced by the de-weighting tower as the heat source of the de-weighting reboiler. Since the heat consumption of the de-weighting tower accounts for more than 80% of the entire multi-effect distillation system, the steam produced by the de-weighting tower is heated by the MVR device to increase the enthalpy and heat it for reboiling at the bottom of the tower, which can greatly reduce the energy consumption of the de-weighting tower and avoid the use of the top condenser to cool and recover the distilled water, thereby reducing the energy consumption and water consumption of the cooling system, and realizing energy saving and water saving in the process of recycling the wastewater from the production of pesticides. The energy transfer equipment or device of the multi-effect distillation system is optimized and designed in combination with the three-dimensional variable space turbulent flow design method, which can reduce the heat transfer end difference of the energy transfer equipment, reduce the power consumption of the energy transfer system, further reduce the energy consumption of the multi-effect distillation system, and realize the low-carbon operation of the multi-effect distillation pesticide production wastewater resource recovery system. The operation reliability and heat exchange performance of the reboiler with a mutually supporting structure without baffles are significantly improved.
附图说明BRIEF DESCRIPTION OF THE DRAWINGS
图1为本实用新型实施例的结构示意图；FIG1 is a schematic structural diagram of an embodiment of the utility model;
图2为本实用新型实施例换热管束采用扭曲椭圆管时的局部结构示意图；FIG2 is a schematic diagram of a local structure of a heat exchange tube bundle using twisted elliptical tubes according to an embodiment of the utility model;
图3为本实用新型实施例换热管束采用扭曲椭圆管时沿横截面方向剖开的剖视图。FIG3 is a cross-sectional view of the heat exchange tube bundle of the embodiment of the utility model when twisted elliptical tubes are used, taken along the cross-sectional direction.
图中附图标记含义：1、原液箱；2、蒸馏水原液加热器；3、冷凝水原液加热器；4、脱轻塔；5、脱轻冷凝器；6、脱轻罐；7、脱轻再沸器；8、脱重塔；9、MVR压缩机；10、MVR降膜再沸器；11、MVR蒸馏水罐；12、精馏塔；13、精馏冷凝器；14、提浓分离罐；15、精馏再沸器；161、原液泵；162、脱轻循环泵；163、脱轻料液泵；164、脱轻采出泵；165、降膜循环泵；166、脱重料液泵；167、蒸馏水回流泵；168、蒸馏水回收泵；169、咪唑烷浓液采出泵；1610、DMF浓液采出泵；1611、强制循环泵；171、脱轻真空泵；172、蒸馏真空泵；181、第一冷凝水回收接口；182、第二冷凝水回收接口；A、原料液；B、不凝气体；C、厂区供热蒸汽；D、厂区回收系统；E、冷却系统；F、生产水洗岗位；G、厂区凝水收集系统。The meanings of the reference numerals in the figure are as follows: 1. stock liquid tank; 2. distilled water stock liquid heater; 3. condensed water stock liquid heater; 4. de-light tower; 5. de-light condenser; 6. de-light tank; 7. de-light reboiler; 8. de-heavy tower; 9. MVR compressor; 10. MVR falling film reboiler; 11. MVR distilled water tank; 12. distillation tower; 13. distillation condenser; 14. concentration separation tank; 15. distillation reboiler; 161. stock liquid pump; 162. de-light circulation pump; 163. de-light feed liquid pump; 164. de-light extraction pump; 165. Membrane circulation pump; 166, deheaving liquid pump; 167, distilled water reflux pump; 168, distilled water recovery pump; 169, imidazolidine concentrate production pump; 1610, DMF concentrate production pump; 1611, forced circulation pump; 171, delightening vacuum pump; 172, distillation vacuum pump; 181, first condensate recovery interface; 182, second condensate recovery interface; A, raw material liquid; B, non-condensable gas; C, plant heating steam; D, plant recovery system; E, cooling system; F, production water washing station; G, plant condensate collection system.
具体实施方式Detailed ways
下面结合附图和具体实施方式对本实用新型的内容做进一步详细说明。The content of the utility model is further described in detail below in conjunction with the accompanying drawings and specific implementation methods.
实施例Example
参阅图1，为一种MVR耦合多效精馏吡虫啉废水资源化回收方法，的方法中包括脱轻塔4、脱重塔8、精馏塔12、MVR压缩机9、MVR降膜再沸器10和MVR蒸馏水罐11，其资源化回收方法包括如下步骤：Referring to FIG1 , a method for recycling wastewater from imidacloprid by MVR coupling multi-effect distillation is shown, wherein the method comprises a light removal tower 4, a heavy removal tower 8, a distillation tower 12, an MVR compressor 9, an MVR falling film reboiler 10 and an MVR distilled water tank 11, and the recycling method comprises the following steps:
步骤一：来自生产车间的农药废水原料液经加热后进入脱轻塔4，在脱轻塔4内减压分离后，在脱轻塔4顶获取的轻组分物质二氯乙烷和甲醇泵送至厂区回收系统D；脱轻塔4中的不凝气体B通过真空泵抽取排出至车间废气处理系统；Step 1: The pesticide wastewater raw material liquid from the production workshop enters the light component removal tower 4 after being heated. After decompression and separation in the light component removal tower 4, the light component substances dichloroethane and methanol obtained at the top of the light component removal tower 4 are pumped to the plant recovery system D; the non-condensable gas B in the light component removal tower 4 is extracted and discharged to the workshop waste gas treatment system through a vacuum pump;
步骤二：将经过脱轻塔4脱轻后的料液泵送至脱重塔8加热进行闪蒸分离，水蒸气进入MVR压缩机9压缩增焓升温后，进入MVR降膜再沸器10壳程释放冷凝潜热后汇集到MVR蒸馏水罐11；脱重塔8闪蒸后的料液和循环料液一起经降膜循环泵165泵至MVR降膜再沸器10管程，吸收壳侧蒸汽释放的潜热后回流至脱重塔；蒸馏水罐收集的蒸馏水被泵送到蒸馏水原液加热器2内进一步释放部分显热，冷却后回到水洗车间回用；Step 2: The liquid after light removal in the light removal tower 4 is pumped to the de-weighting tower 8 for heating and flash separation. After the water vapor enters the MVR compressor 9 for compression and enthalpy increase and temperature rise, it enters the MVR falling film reboiler 10 shell side to release the condensation latent heat and then is collected in the MVR distilled water tank 11; the liquid after flash evaporation in the de-weighting tower 8 and the circulating liquid are pumped to the MVR falling film reboiler 10 tube side through the falling film circulation pump 165, and then reflux to the de-weighting tower after absorbing the latent heat released by the shell side steam; the distilled water collected in the distilled water tank is pumped to the distilled water stock heater 2 to further release part of the sensible heat, and then returned to the washing workshop for reuse after cooling;
步骤三：脱重塔8底部采出部分富含有咪唑烷和DMF的料液，经过蒸馏后泵送至精馏塔12内减压蒸馏，精馏后蒸出DMF和少部分水蒸气泵送至厂区回收系统D生产线套用，余下富含咪唑烷的母液经冷却回收咪唑烷回生产线套用。Step 3: A portion of the feed liquid rich in imidazolidine and DMF is extracted from the bottom of the deweighting tower 8, and after distillation, it is pumped to the distillation tower 12 for vacuum distillation. After distillation, DMF and a small amount of water vapor are evaporated and pumped to the plant recovery system D production line for application. The remaining mother liquor rich in imidazolidine is cooled to recover the imidazolidine and return it to the production line for application.
本回收方法中，其目的是利用吡虫啉的二氯乙烷溶液中溶解的咪唑烷通过溶解度的不同，将咪唑烷溶解到热水中，溶解咪唑烷后的热水中同时有DMF及二氯乙烷和甲醇等杂质，采用多级精馏工艺回收DMF和咪唑烷。在脱轻塔4的塔顶除去二氯乙烷和甲醇等轻组份；脱轻塔4底采出含有DMF和咪唑烷的热水再去脱重塔8，在脱重塔8采用MVR蒸馏方式，塔顶采出蒸汽通过MVR压缩机9压缩增焓后回到塔底MVR降膜再沸器10，为释放潜热塔底再沸腾提供热量，蒸馏水再进原料液加热器进一步释放潜热后回生产水洗岗位F循环套用；脱重塔8底采出含有咪唑烷和DMF的母液，经精馏后蒸出DMF去生产线套用，余下的母液经冷却回收咪唑烷回生产线套用。In this recovery method, the purpose is to utilize the imidazolidine dissolved in the dichloroethane solution of imidacloprid to dissolve the imidazolidine in hot water through different solubility. The hot water after dissolving the imidazolidine contains impurities such as DMF, dichloroethane and methanol at the same time, and a multi-stage distillation process is used to recover DMF and imidazolidine. The light components such as dichloroethane and methanol are removed at the top of the light removal tower 4; the hot water containing DMF and imidazolidine is extracted from the bottom of the light removal tower 4 and then goes to the heavy removal tower 8. The heavy removal tower 8 adopts the MVR distillation method, and the steam extracted from the top of the tower is compressed by the MVR compressor 9 to increase the enthalpy and then returns to the MVR falling film reboiler 10 at the bottom of the tower to provide heat for releasing the latent heat and reboiling at the bottom of the tower. The distilled water enters the raw material liquid heater to further release the latent heat and then returns to the production water washing station F for recycling; the mother liquor containing imidazolidine and DMF is extracted from the bottom of the heavy removal tower 8, and DMF is evaporated after distillation and applied to the production line, and the remaining mother liquor is cooled to recover the imidazolidine and return to the production line for application.
一种实现MVR耦合多效精馏吡虫啉废水资源化回收装置，装置包括原液箱1、二级原液加热器、原液泵161、脱轻冷凝器5、脱轻罐6、脱轻再沸器7、脱轻循环泵162、脱轻料液泵163和脱轻采出泵164；脱轻塔4前设置有原液箱1和二级原液加热器，二级原液加热器的热源分别来自回收的MVR蒸馏水和脱轻塔4及精馏塔12的冷凝水显热；二级原液加热器包括蒸馏水原液加热器2和与其相连的冷凝水原液加热器3；原液箱1进口与来自生产车间的原料液A通过连接管道连接，原液泵161的入口与原液箱1相连，原液泵161的出口与蒸馏水原液加热器2相连；脱轻塔4塔顶与脱轻冷凝器5、脱轻罐6分别连接，脱轻塔4底部通过脱轻循环泵162与脱轻再沸器7底部管程相连，脱轻再沸器7上部管程与脱轻塔4下部相连；脱轻冷凝器5与脱轻罐6还连接有用于抽出脱轻塔4内不凝气体B的脱轻真空泵171；脱轻罐6底部通过脱轻采出泵164与厂区回收系统D连接；脱轻塔4底部通过脱轻料液泵163与脱重塔8相连；脱轻再沸器7的热源来自厂区供热蒸汽C，脱轻再沸器7通过第二冷凝水回收接口182与冷凝水原液加热器3连接；加热蒸汽走壳程，释放潜热后通过第二冷凝水回收接口182与冷凝水原液加热器3连接，并在冷凝水原液加热器3内进一步释放显热后回收利用。从脱轻塔4塔顶蒸出的轻组份在脱轻冷凝器5冷凝，一部分回流到脱轻塔4，另一部分进入脱轻罐6后回收；脱轻塔4塔底有脱轻再沸器7，热源来自厂区供热蒸汽C，加热蒸汽走壳程，释放潜热后经第二冷凝水回收接口182送至冷凝水原液加热器3，进一步释放显热后回到厂区凝水收集系统G；脱轻塔4底设有出料泵(脱轻料液泵163)采出含有DMF和咪唑烷的热水至脱重塔8。本实施例中，脱轻真空泵171的设置，在抽出脱轻塔4不凝性气体的同时确保系统真空运行。A device for recycling imidacloprid wastewater by MVR coupling and multi-effect distillation, the device comprising a stock liquid tank 1, a secondary stock liquid heater, a stock liquid pump 161, a light removal condenser 5, a light removal tank 6, a light removal reboiler 7, a light removal circulation pump 162, a light removal feed liquid pump 163 and a light removal extraction pump 164; a stock liquid tank 1 and a secondary stock liquid heater are arranged in front of a light removal tower 4, and the heat sources of the secondary stock liquid heater come from the recovered MVR distilled water and the sensible heat of the condensed water of the light removal tower 4 and the distillation tower 12 respectively; the secondary stock liquid heater comprises a distilled water stock liquid heater 2 and a condensed water stock liquid heater 3 connected thereto; the inlet of the stock liquid tank 1 is connected to the raw material liquid A from the production workshop through a connecting pipe, the inlet of the stock liquid pump 161 is connected to the stock liquid tank 1, and the outlet of the stock liquid pump 161 is connected to the distilled water stock liquid heater 2; the top of the light removal tower 4 is connected to the light removal condenser The de-lightening tower 4 is connected to the bottom of the de-lightening tower 4 through a de-lightening circulation pump 162 and the bottom pipe side of the de-lightening reboiler 7, and the upper pipe side of the de-lightening reboiler 7 is connected to the lower part of the de-lightening tower 4; the de-lightening condenser 5 and the de-lightening tank 6 are also connected with a de-lightening vacuum pump 171 for extracting the non-condensable gas B in the de-lightening tower 4; the bottom of the de-lightening tank 6 is connected to the plant recovery system D through a de-lightening extraction pump 164; the bottom of the de-lightening tower 4 is connected to the de-heavy tower 8 through a de-lightening liquid pump 163; the heat source of the de-lightening reboiler 7 comes from the plant heating steam C, and the de-lightening reboiler 7 is connected to the condensate stock liquid heater 3 through a second condensate recovery interface 182; the heating steam goes through the shell side, and after releasing the latent heat, it is connected to the condensate stock liquid heater 3 through the second condensate recovery interface 182, and is further released in the condensate stock liquid heater 3. Recyclable. The light components evaporated from the top of the light removal tower 4 are condensed in the light removal condenser 5, a part of which flows back to the light removal tower 4, and the other part enters the light removal tank 6 for recovery; there is a light removal reboiler 7 at the bottom of the light removal tower 4, and the heat source comes from the heating steam C in the plant area. The heating steam goes through the shell side, and after releasing the latent heat, it is sent to the condensate stock heater 3 through the second condensate recovery interface 182, and returns to the condensate collection system G in the plant area after further releasing the sensible heat; a discharge pump (light removal liquid pump 163) is provided at the bottom of the light removal tower 4 to extract hot water containing DMF and imidazolidine to the heavy removal tower 8. In this embodiment, the light removal vacuum pump 171 is set to ensure the vacuum operation of the system while extracting the non-condensable gas in the light removal tower 4.
装置还包括降膜循环泵165、脱重料液泵166、蒸馏水回流泵167、蒸馏水回收泵168和第一冷凝水回收接口181；脱重塔8顶部与MVR压缩机9连接，MVR压缩机9与MVR降膜再沸器10上部壳程连接；MVR降膜再沸器10底部管程与脱重塔8下部连接，MVR降膜再沸器10管程顶部通过降膜循环泵165与脱重塔8底部连接；MVR降膜再沸器10壳程底部与MVR蒸馏水罐11相连，MVR蒸馏水罐11出口依次通过蒸馏水回收泵168、第一冷凝水回收接口181与蒸馏水原液加热器2连接，MVR蒸馏水罐11出口还通过蒸馏水回流泵167与脱重塔8上部连接；脱重塔8底部通过脱重料液泵166与精馏塔12连接。脱重塔8塔顶蒸汽先进入MVR压缩机9，增焓升温后进入塔底MVR降膜再沸器10壳侧，释放潜热后再进入MVR蒸馏水罐11；脱重塔8塔底设有降膜循环泵165，将物料泵入MVR降膜再沸器10，在加热器管内降膜加热后回流至脱重塔8；MVR蒸馏水罐11收集MVR降膜再沸器10的冷凝水，一部分回流至脱重塔8塔顶，另一部分泵送至蒸馏水原液加热器2，进一步释放显热后回生产水洗岗位F循环套用；脱重塔8塔底还设有脱重料液泵166，将富含有咪唑烷和DMF的母液泵至精馏塔12。The device also includes a falling film circulation pump 165, a deweighting liquid pump 166, a distilled water reflux pump 167, a distilled water recovery pump 168 and a first condensed water recovery interface 181; the top of the deweighting tower 8 is connected to the MVR compressor 9, and the MVR compressor 9 is connected to the upper shell side of the MVR falling film reboiler 10; the bottom tube side of the MVR falling film reboiler 10 is connected to the lower part of the deweighting tower 8, and the top of the tube side of the MVR falling film reboiler 10 is connected to the bottom of the deweighting tower 8 through the falling film circulation pump 165; the bottom of the shell side of the MVR falling film reboiler 10 is connected to the MVR distilled water tank 11, and the outlet of the MVR distilled water tank 11 is connected to the distilled water stock liquid heater 2 through the distilled water recovery pump 168 and the first condensed water recovery interface 181 in sequence, and the outlet of the MVR distilled water tank 11 is also connected to the upper part of the deweighting tower 8 through the distilled water reflux pump 167; the bottom of the deweighting tower 8 is connected to the distillation tower 12 through the deweighting liquid pump 166. The steam from the top of the de-weighting tower 8 first enters the MVR compressor 9, and after increasing enthalpy and heating, enters the shell side of the MVR falling film reboiler 10 at the bottom of the tower, and then enters the MVR distilled water tank 11 after releasing latent heat; a falling film circulation pump 165 is provided at the bottom of the de-weighting tower 8 to pump the material into the MVR falling film reboiler 10, and the material is refluxed to the de-weighting tower 8 after falling film heating in the heater tube; the MVR distilled water tank 11 collects the condensed water of the MVR falling film reboiler 10, part of which is refluxed to the top of the de-weighting tower 8, and the other part is pumped to the distilled water stock liquid heater 2, and after further releasing sensible heat, it is returned to the production water washing station F for circulation; a de-weighting liquid pump 166 is also provided at the bottom of the de-weighting tower 8 to pump the mother liquor rich in imidazolidine and DMF to the distillation tower 12.
装置还包括精馏冷凝器13、提浓分离罐14、精馏再沸器15、DMF浓液采出泵1610、咪唑烷浓液采出泵169、强制循环泵1611和蒸馏真空泵172；精馏塔12顶部出口与精馏冷凝器13连接，提浓分离罐14与精馏塔12上部进口连接，精馏冷凝器13的一出口通过连接管连接在提浓分离罐14与精馏塔12之间的连接管路上；提浓分离罐14与精馏冷凝器13并接在蒸馏真空泵172上，并通过蒸馏真空泵172与车间废气处理系统连接；提浓分离罐14底部通过DMF浓液采出泵1610与厂区回收系统D连接；精馏塔12底部通过强制循环泵1611与精馏再沸器15底部管程连接，精馏再沸器15管程顶部与精馏塔12下部连接，精馏再沸器15下部壳程通过第二冷凝水回收接口182与冷凝水原液加热器3连接，精馏再沸器15的热源来自厂区供热蒸汽C并进入精馏再沸器15壳程；精馏塔12底部通过咪唑烷浓液采出泵169送回生产线套用。从精馏塔12塔顶精馏冷凝器13蒸出的DMF蒸汽，一部分回流到精馏塔12，另一部分进入提浓分离罐14后回收再利用；精馏塔12塔底有精馏再沸器15，热源来自厂区供热蒸汽，第二冷凝水回收接口182送至冷凝水原液加热器3，释放显热后回到厂区凝水收集系统G；精馏塔12底设有出料泵(咪唑烷浓液采出泵169)采出富含咪唑烷的浓液泵送至回生产线套用。本实施例中，蒸馏真空泵172的设置，在抽出精馏塔12不凝性气体的同时确保系统真空运行。The device also includes a distillation condenser 13, a concentration separation tank 14, a distillation reboiler 15, a DMF concentrate extraction pump 1610, an imidazolidine concentrate extraction pump 169, a forced circulation pump 1611 and a distillation vacuum pump 172; the top outlet of the distillation tower 12 is connected to the distillation condenser 13, the concentration separation tank 14 is connected to the upper inlet of the distillation tower 12, and an outlet of the distillation condenser 13 is connected to the connecting pipeline between the concentration separation tank 14 and the distillation tower 12 through a connecting pipe; the concentration separation tank 14 and the distillation condenser 13 are connected to the distillation vacuum pump 172 in parallel, and are connected to the workshop through the distillation vacuum pump 172 The exhaust gas treatment system is connected; the bottom of the concentration separation tank 14 is connected to the plant recovery system D through the DMF concentrate extraction pump 1610; the bottom of the distillation tower 12 is connected to the bottom pipe side of the distillation reboiler 15 through the forced circulation pump 1611, the top of the distillation reboiler 15 pipe side is connected to the lower part of the distillation tower 12, and the lower shell side of the distillation reboiler 15 is connected to the condensate stock heater 3 through the second condensate recovery interface 182. The heat source of the distillation reboiler 15 comes from the plant heating steam C and enters the distillation reboiler 15 shell side; the bottom of the distillation tower 12 is sent back to the production line for application through the imidazolidine concentrate extraction pump 169. A portion of the DMF steam evaporated from the rectifying condenser 13 at the top of the rectifying tower 12 flows back to the rectifying tower 12, and the other portion enters the concentration separation tank 14 for recycling; a rectifying reboiler 15 is provided at the bottom of the rectifying tower 12, and the heat source comes from the heating steam in the plant area, and the second condensed water recovery interface 182 is sent to the condensed water stock heater 3, and returns to the condensed water collection system G in the plant area after releasing the sensible heat; a discharge pump (imidazolidine concentrate extraction pump 169) is provided at the bottom of the rectifying tower 12 to extract the concentrate rich in imidazolidine and pump it back to the production line for application. In this embodiment, the setting of the distillation vacuum pump 172 ensures the vacuum operation of the system while extracting the non-condensable gas of the rectifying tower 12.
本实施例中，来自生产车间的原料液A(此例为吡虫啉生产水洗工序废水)先经过原液箱1，再由原液泵161送至蒸馏水原液加热器2，升温后继续进入冷凝水原液加热器3进行二次加热，再进入脱轻塔4。加热后的原料液A进入脱轻塔4后，与脱轻塔4内的料液一起在脱轻循环泵162的作用下进入脱轻再沸器7，受热后回到脱轻塔4，此时高温的料液进入脱轻塔4后减压分离，二氯乙烷和甲醇等轻组份蒸发，同时含部分水蒸气，一并进入塔顶脱轻冷凝器5和脱轻罐6进行分离，同时部分冷凝液回流至脱轻塔4塔顶；脱轻系统的不凝性气体通过脱轻真空泵171抽取排出至车间废气处理系统，脱轻罐6底连接脱轻塔4的脱轻采出泵164，将采出的轻组份泵送至厂区回收系统D。In this embodiment, the raw material liquid A from the production workshop (in this case, the wastewater from the washing process of imidacloprid production) first passes through the raw liquid tank 1, and then is sent to the distilled water raw liquid heater 2 by the raw liquid pump 161. After heating, it continues to enter the condensed water raw liquid heater 3 for secondary heating, and then enters the light removal tower 4. After the heated raw material liquid A enters the light removal tower 4, it enters the light removal reboiler 7 under the action of the light removal circulation pump 162 together with the feed liquid in the light removal tower 4, and returns to the light removal tower 4 after being heated. At this time, the high-temperature feed liquid enters the light removal tower 4 and is decompressed and separated, and light components such as dichloroethane and methanol evaporate, and at the same time contain part of the water vapor, and enter the light removal condenser 5 and the light removal tank 6 at the top of the tower for separation, and at the same time, part of the condensate refluxes to the top of the light removal tower 4; the non-condensable gas of the light removal system is extracted and discharged to the workshop waste gas treatment system by the light removal vacuum pump 171, and the light removal extraction pump 164 of the light removal tower 4 is connected to the bottom of the light removal tank 6, and the extracted light components are pumped to the plant area recovery system D.
脱轻塔4底部的脱轻料液泵163，将脱轻后的料液泵送至脱重塔8，料液进入脱重塔8后部分水分蒸发，其余进入提馏段，经降膜循环泵165泵送至MVR降膜再沸器10顶部，经过管侧降膜加热后回到脱重塔8下部；受热后的料液进入脱重塔8后闪蒸分离，其中水蒸气从塔顶进入MVR压缩机9，被压缩增焓升温后进入MVR降膜再沸器10壳侧，释放潜热后冷凝，蒸馏水进入MVR蒸馏水罐11后，一部分通过蒸馏水回收泵168泵送至蒸馏水原液加热器2，进一步释放部分显热冷却后回到水洗车间回用；另一部分被蒸馏水回流泵167泵回到脱重塔8的塔顶。The light-removal liquid pump 163 at the bottom of the light-removal tower 4 pumps the light-removal liquid to the de-weighting tower 8. After the liquid enters the de-weighting tower 8, part of the water evaporates, and the rest enters the stripping section, and is pumped to the top of the MVR falling film reboiler 10 by the falling film circulation pump 165, and returns to the lower part of the de-weighting tower 8 after being heated by the falling film on the tube side; the heated liquid enters the de-weighting tower 8 and is flash-evaporated and separated, wherein the water vapor enters the MVR compressor 9 from the top of the tower, is compressed to increase the enthalpy and heat, and then enters the shell side of the MVR falling film reboiler 10, condenses after releasing the latent heat, and after the distilled water enters the MVR distilled water tank 11, a part of it is pumped to the distilled water stock liquid heater 2 by the distilled water recovery pump 168, further releases part of the sensible heat, and then returns to the washing workshop for reuse after cooling; the other part is pumped back to the top of the de-weighting tower 8 by the distilled water reflux pump 167.
轻重塔底部的脱重料液泵166，将蒸馏后的料液泵送至精馏塔12，料液进入精馏塔12后与循环料液一起进入强制循环泵1611，通过强制循环泵1611将料液泵入精馏再沸器15，受热后回到精馏塔12，此时高温的料液进入精馏塔12后减压精馏，DMF和部分水蒸气进入精馏冷凝器13和提浓分离罐14，同时部分冷凝液回流至精馏塔12塔顶；脱轻系统的不凝性气体通过脱轻真空泵171抽取排出至车间废气处理系统，提浓分离罐14底连接DMF浓液采出泵1610，将采出的DMF浓液泵送至厂区回收系统D；精馏塔12底部设置有咪唑烷浓液采出泵169，将脱除DMF后的料液泵送至水洗车间回用。The de-heavy liquid pump 166 at the bottom of the light-heavy tower pumps the distilled liquid to the distillation tower 12. After entering the distillation tower 12, the liquid enters the forced circulation pump 1611 together with the circulating liquid. The liquid is pumped into the distillation reboiler 15 by the forced circulation pump 1611, and returns to the distillation tower 12 after being heated. At this time, the high-temperature liquid enters the distillation tower 12 and is vacuum-distilled. DMF and part of the water vapor enter the distillation condenser 13 and the concentration separation tank 14, and part of the condensate flows back to the top of the distillation tower 12; the non-condensable gas of the de-light system is extracted and discharged to the workshop waste gas treatment system by the de-light vacuum pump 171, and the bottom of the concentration separation tank 14 is connected to the DMF concentrate extraction pump 1610, and the extracted DMF concentrate is pumped to the plant recovery system D; an imidazolidine concentrate extraction pump 169 is provided at the bottom of the distillation tower 12 to pump the liquid after the DMF is removed to the washing workshop for reuse.
本实施例的一种MVR耦合多效精馏吡虫啉生产水洗工序废水资源化回收方法，目的是开发一种耦合MVR热泵的多效精馏处理农药生产废水资源化回收的方法技术，并结合三维顺紊流热交换设备的设计方法，最大限度的利用多效精馏过程的余热，提升多效精馏处理农药生产废水资源化回收的能量利用水平，从而大大降低废水资源化回收用能成本；采用三维顺紊流热交换设备的设计方法对多效精馏系统的热交换设备或装置进行优化设计，结合扭曲椭圆管自支撑结构设计和并行流热交换形式，可以最大限度的缩小换热端差，提高热交换装置的换热效率，提高热交换装置的运行可靠性。The present embodiment provides a method for resource recovery of wastewater from the washing process of imidacloprid production by MVR-coupled multi-effect distillation, with the aim of developing a method technology for resource recovery of pesticide production wastewater by multi-effect distillation coupled with an MVR heat pump, and combining the design method of a three-dimensional turbulent flow heat exchange device to maximize the use of waste heat from the multi-effect distillation process, thereby improving the energy utilization level of resource recovery of pesticide production wastewater by multi-effect distillation, and thus greatly reducing the energy cost of wastewater resource recovery; the design method of a three-dimensional turbulent flow heat exchange device is used to optimize the design of the heat exchange equipment or device of the multi-effect distillation system, and combined with the twisted elliptical tube self-supporting structure design and the parallel flow heat exchange form, the heat exchange end difference can be minimized to the maximum extent, the heat exchange efficiency of the heat exchange device can be improved, and the operating reliability of the heat exchange device can be improved.
本实施例的MVR耦合多效精馏吡虫啉生产水洗工序废水资源化回收方法，与以多效精馏或单效MVR热泵蒸馏为代表的蒸馏系统相比，由于采用了三维顺紊流设计及优化方法的热交换设备，可以缩小MVR热交换设备的换热温压，降低MVR压缩功耗，最大限度的利用精馏系统的废热资源，大大提升废水资源化回收用能水平。以本实施案例为例，采用了MVR耦合多效精馏吡虫啉生产水洗工序废水资源化回收工艺后，单位咪唑烷回收能耗，较传统单效蒸馏系统降低75％以上；较传统三效精馏吡虫啉生产水洗工序废水资源化回收工艺，单位咪唑烷回收能耗降低30％～50％；此外，由于采用了MVR技术，无需采出水冷凝器，大大减少了冷却系统的能耗和水耗。因此，本实施例可以有效降低吡虫啉生产水洗工序废水资源化回收能耗，实现农药废水低碳资源化回收。The MVR coupled multi-effect distillation method for recycling wastewater from the washing process of imidacloprid production in this embodiment is compared with the distillation system represented by multi-effect distillation or single-effect MVR heat pump distillation. Due to the use of heat exchange equipment with three-dimensional turbulent design and optimization method, the heat exchange temperature and pressure of the MVR heat exchange equipment can be reduced, the MVR compression power consumption can be reduced, and the waste heat resources of the distillation system can be used to the maximum extent, which greatly improves the energy level of wastewater recycling. Taking this implementation case as an example, after adopting the MVR coupled multi-effect distillation wastewater recycling process for the washing process of imidacloprid production, the unit imidazoline recycling energy consumption is reduced by more than 75% compared with the traditional single-effect distillation system; compared with the traditional three-effect distillation wastewater recycling process for the washing process of imidacloprid production, the unit imidazoline recycling energy consumption is reduced by 30% to 50%; in addition, due to the use of MVR technology, no water condenser is required, which greatly reduces the energy consumption and water consumption of the cooling system. Therefore, this embodiment can effectively reduce the energy consumption of wastewater recycling in the washing process of imidacloprid production, and realize low-carbon recycling of pesticide wastewater.
本实施例中，脱轻冷凝器5与精馏冷凝器13均与冷却系统E连接。In this embodiment, the light removal condenser 5 and the rectification condenser 13 are both connected to the cooling system E.
MVR降膜再沸器10采用扭曲椭圆管作为加热器换热管束，MVR降膜再沸器10的筒体内设置有用于包裹换热管束的导流筒。The MVR falling film reboiler 10 uses twisted elliptical tubes as the heater heat exchange tube bundle. A guide tube for wrapping the heat exchange tube bundle is arranged in the cylinder of the MVR falling film reboiler 10 .
脱轻再沸器7和精馏再沸器15均采用扭曲椭圆管并行设置的换热管束；蒸馏水原液加热器2和冷凝水原液加热器3采用扭曲椭圆管管壳式换热器或板式换热器。The light removal reboiler 7 and the distillation reboiler 15 both use heat exchange tube bundles with twisted elliptical tubes arranged in parallel; the distilled water stock heater 2 and the condensed water stock heater 3 use twisted elliptical tube shell and tube heat exchangers or plate heat exchangers.
脱轻塔4与脱重塔8均采用板式塔结构，精馏塔12采用板式塔结构或填料塔结构。The light-removal tower 4 and the heavy-removal tower 8 both adopt a plate tower structure, and the distillation tower 12 adopts a plate tower structure or a packed tower structure.
管壳式加热器与再沸器的换热管束由若干高比表面的扭曲椭圆管通过捆扎并使得管束间形成凸点接触而构成相互支撑结构，形成轴向多通道的流通通道，无需设折流板或中间支撑管板；扭曲椭圆管的横截面为近椭圆形，经过二次加工扭曲形成螺旋状结构。换热管束之间形成轴向多通道的三维变空间顺紊流设计，可缩小换热端差，降低能量损耗，提高热交换效率。换热管束采用高比表面的扭曲椭圆管，扭曲椭圆管之间通过凸点接触相互支撑形成的稳定结构，换热效果好，有利于热量的回收。换热管束之间形成轴向多通道的三维变空间顺紊流设计，近椭圆形的横截面设计的扭曲椭圆管，使得在三维变空间内无死角流动，不存在涡流点，不存在磨损角，不会形成结垢、积灰的情况。The heat exchange tube bundles of the shell and tube heater and the reboiler are composed of several twisted elliptical tubes with high specific surface area, which are bundled and form convex contact between the tube bundles to form a mutual support structure, forming an axial multi-channel flow channel, without the need for baffles or intermediate support tube sheets; the cross-section of the twisted elliptical tube is nearly elliptical, and is twisted to form a spiral structure after secondary processing. The three-dimensional variable space turbulent flow design with axial multi-channels between the heat exchange tube bundles can reduce the heat exchange end difference, reduce energy loss, and improve heat exchange efficiency. The heat exchange tube bundle adopts twisted elliptical tubes with high specific surface area. The twisted elliptical tubes are mutually supported by convex contact to form a stable structure, which has good heat exchange effect and is conducive to heat recovery. The three-dimensional variable space turbulent flow design with axial multi-channels between the heat exchange tube bundles and the twisted elliptical tubes with a nearly elliptical cross-section design make the flow in the three-dimensional variable space without dead angles, eddy points, wear angles, and scaling and dust accumulation.
关于换热管使用，参阅图2至图3，图2中只展示了单根扭曲椭圆管，若是多根扭曲椭圆管并列设置时，相邻扭曲椭圆管之间通过凸出的凸点形成支撑。Regarding the use of heat exchange tubes, please refer to Figures 2 to 3. Figure 2 only shows a single twisted elliptical tube. If multiple twisted elliptical tubes are arranged in parallel, support is formed between adjacent twisted elliptical tubes through protruding bumps.
上列详细说明是针对本实用新型可行实施例的具体说明，该实施例并非用以限制本实用新型的专利范围，凡未脱离本实用新型所为的等效实施或变更，均应包含于本案的专利范围中。The above detailed description is a specific description of a feasible embodiment of the utility model. The embodiment is not intended to limit the patent scope of the utility model. Any equivalent implementation or modification that does not deviate from the utility model should be included in the patent scope of this case.
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