CN208843875U - 一种高含盐含溶剂废水处理系统 - Google Patents
一种高含盐含溶剂废水处理系统 Download PDFInfo
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- CN208843875U CN208843875U CN201820108558.5U CN201820108558U CN208843875U CN 208843875 U CN208843875 U CN 208843875U CN 201820108558 U CN201820108558 U CN 201820108558U CN 208843875 U CN208843875 U CN 208843875U
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- 239000002904 solvent Substances 0.000 title claims abstract description 28
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 11
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 238000004821 distillation Methods 0.000 claims abstract description 26
- 239000011552 falling film Substances 0.000 claims abstract description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 239000012452 mother liquor Substances 0.000 claims description 15
- 239000003507 refrigerant Substances 0.000 claims description 12
- 239000010408 film Substances 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 24
- 238000010612 desalination reaction Methods 0.000 abstract description 8
- 239000002918 waste heat Substances 0.000 abstract description 4
- 239000012071 phase Substances 0.000 description 13
- 239000002002 slurry Substances 0.000 description 13
- 238000001704 evaporation Methods 0.000 description 11
- 238000000034 method Methods 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 7
- 239000011780 sodium chloride Substances 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 6
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-dimethylformamide Chemical compound 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- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound 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- UIIMBOGNXHQVGW-UHFFFAOYSA-M NaHCO3 Chemical compound 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[Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 1
- QNEFNFIKZWUAEQ-UHFFFAOYSA-N carbonic acid;potassium Chemical compound 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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Abstract
本实用新型公开了一种高含盐含溶剂废水处理系统，原水泵出口依次与第一换热器和第二换热器相连；内盘管蒸发器的出气口通过气相管道与第一精馏塔相连，第一精馏塔通过管道依次与第二精馏塔和第三精馏塔相连，第一精馏塔的蒸汽出口与第一换热器的热媒进口相连，第二精馏塔的蒸汽出口与降膜蒸发器的蒸汽进口相连；内盘管蒸发器出液口相连有两路分支管，一路分支管与降膜蒸发器的进料口相连，降膜蒸发器的出气口连接有气液分离器，气液分离器的出气管并入气相管道，另一路分支管通过第二换热器与离心机相连，离心机通过输送泵回连至内盘管蒸发器上部的进液口。本实用新型不但实现了连续化除盐精馏，回收得到的溶剂纯度高，而且余热得到充分回收利用。
Description
技术领域
本实用新型涉及一种高含盐含溶剂废水处理系统。
背景技术
目前高含盐含溶剂废脱盐方法主要分为膜法和热法，膜法主要以反渗透、纳滤、渗透汽化及电渗析为主，首先通过膜过滤掉溶剂，然后通过膜过滤脱盐；该方法能耗低，系统安装维护相对简单，但由于其易污染且寿命短，需要频繁清洗和更换膜材料，脱盐成本高，且大部分有机膜材料不能用于含有机溶剂或较高温度的含盐废水处理。
因此，目前工业化使用较多是热法，热法包括多级闪蒸、低温多效蒸馏及压汽蒸馏等，如三效装置，蒸出水，然后除盐离心，盐烘干处理，离心母液去精馏溶剂回用，该方法需要装置配套齐全且人工操作量大，同时离心母液由于含部分盐分及其他焦油类物质，导致精馏也需要除盐装置，且母液由于含有焦油故需要及时排放保证系统的稳定，系统复杂，操作要求高，连续性自动性不强。
工业生产中产生的高含盐含溶剂废水制约着生产，因此考虑处理成本，环保，安全，投入资金等各方面综合因素，设计出节能高效、技术先进、减少污染、安全可操作的工艺装置，对于精细化工行业贡献巨大，提高企业和行业的社会和经济效益，促进行业可持续发展，具有重大现实意义。
实用新型内容
本实用新型提供了一种高含盐含溶剂废水处理系统，不但实现了连续化除盐精馏，回收得到的溶剂纯度高，且充分利用整套系统热能，无三废产出。
为了解决上述问题，本实用新型所采用的技术方案是这样的，一种高含盐含溶剂废水处理系统，包括第一换热器、第二换热器、内盘管蒸发器，降膜蒸发器，离心机，第一精馏塔、第二精馏塔和第三精馏塔，原水泵出口与第一换热器的冷媒进口相连，第一换热器的冷媒出口与第二换热器的冷媒进口相连，第二换热器的冷媒出口与内盘管蒸发器上部的进液口相连；内盘管蒸发器顶部的出气口通过气相管道与第一精馏塔进料口相连，第一精馏塔的釜底出液口与第二精馏塔的进料口相连，第二精馏塔的釜底出液口与第三精馏塔的进料口相连，第一精馏塔的蒸汽出口与第一换热器的热媒进口相连，第二精馏塔的蒸汽出口与降膜蒸发器的蒸汽进口相连；内盘管蒸发器底部的出液口通过循环泵与两路分支管相连，其中，一路分支管与降膜蒸发器的进料口相连，降膜蒸发器的出液口回连至内盘管蒸发器上部的进液口，降膜蒸发器的出气口连接有气液分离器，气液分离器的出气管并入连接内盘管蒸发器出气口与第一精馏塔进料口的气相管道，另一路分支管与第二换热器的热媒进口相连，第二换热器的热媒出口与离心机进料口相连，离心机的出液口与母液槽的进料口相连，母液槽的出料口通过输送泵回连至内盘管蒸发器上部的进液口。
优选地，气液分离器的出液管回连至降膜蒸发器的进料口。
离心机和母液槽的尾气出口管与尾气吸收装置相连。尾气得到收集，无气味逸散，更加环保，同时增加了系统的安全性。
有益效果：
1、本系统充分利用第一精馏塔高温蒸汽和待离心的高温料浆液的自身的热量，从而使得整个系统的余热综合利用，热效率得到提高，热量最大化利用，能耗回用率高。
2、本系统利用内盘管蒸发器+降膜蒸发器处理原水，蒸发量大，蒸发效率高，能耗利用率高，处理能力大。另外利用第二精馏塔的蒸汽气相对降膜蒸发器内浆液进行蒸发，系统的余热得到最大化的充分利用。
3、本系统离心自动连续操作，提高了利用率及产能，且节省人力。
4、本系统回收得到的溶剂纯度高，可直接回用，蒸出蒸汽水的余热被利用(对原水进行初预热和对降膜蒸发器内浆液进行蒸发)后变成冷凝水直接外排或回收套用，环保。
综上，本系统不但能够高效处理含盐含溶剂废水，余热得到充分回收利用，同时无三废产出，自动化程度高，不需要人工及输送系统进转料操作，且对蒸发回收溶剂水进行精馏，溶剂纯度高，能够完全回用，相对于现有热法-含盐含溶剂废水处理工艺(三效装置蒸出水，然后离心除盐，盐烘干处理，离心母液进行溶剂精馏具有如下优势，具体见表1所示：
表1
。
附图说明
图1是本实用新型结构示意图；
图2为本实用新型流程图。
具体实施方式
为了加深对本实用新型的理解，下面将结合实施例和附图对本实用新型作进一步详述，该实施例仅用于解释本实用新型，并不构成对本实用新型保护范围的限定。
参见图1，一种高含盐含溶剂废水处理系统，包括第一换热器1、第二换热器2、内盘管蒸发器3，降膜蒸发器4，离心机5，第一精馏塔6、第二精馏塔7和第三精馏塔8，原水泵12出口与第一换热器1的冷媒进口相连，第一换热器 1的冷媒出口与第二换热器2的冷媒进口相连，第二换热器的2冷媒出口与内盘管蒸发器3上部的进液口相连；内盘管蒸发器3部的出气口通过气相管道与第一精馏塔6进料口相连，第一精馏塔6的釜底出液口与第二精馏塔7的进料口相连，第二精馏塔7的釜底出液口与第三精馏塔8的进料口相连，第一精馏塔6的蒸汽出口与第一换热器1的热媒进口相连，第二精馏塔8的蒸汽出口与降膜蒸发器4 的蒸汽进口相连；内盘管蒸发器3底部的出液口通过循环泵与两路分支管相连，其中，一路分支管与降膜蒸发器4的进料口相连，降膜蒸发器4的出液口回连至内盘管蒸发器上部的进液口，降膜蒸发器4的出气口连接有气液分离器9，气液分离器9的出气管并入连接内盘管蒸发器3出气口与第一精馏塔6进料口的气相管道，气液分离器9的出液管与降膜蒸发器4的进料口回连；另一路分支管与第二换热器2的热媒进口相连，第二换热器2的热媒出口与离心机5的进料口相连，离心机5的出液口于母液槽11的进料口相连，母液槽11的出料口通过输送泵回连至内盘管蒸发器3上部的进液口。
其中，离心机5和母液槽11的尾气出口管与尾气吸收装置10相连。
本系统可利用现有热法含盐含溶剂废水处理设备改装实现，放弃使用现有的三效装置，增加一台降膜蒸发器和2台换热器，内盘管蒸发器可通过在现有的蒸馏釜内增设内盘管来实现，整套系统新增投入少。
利用上述系统具体处理高含盐含溶剂废水的工艺方法，包括如下步骤：利用上述系统处理高含盐含溶剂废水的工艺方法，包括如下步骤：
1)将常温条件下DMF含盐废水(废水中溶剂DMF含量为22-25wt％，总含盐量25wt％，焦油类有机杂质1wt％，其余均为水；其中，盐包括碳酸钾98wt％、微量碳酸氢钾和氯化钾，合计1wt％和其他杂质1wt％)，经原水泵送入第一换热器(进水量通过流量计控制，保证在2500kg/h的流量)与从第一精馏塔采出的高温蒸汽气相进行换热(换热后水温度为35℃)，初预热后原水进入第二换热器，与从内盘管蒸发器出的待离心高温浆液二次换热(二次换热后原水温度为 40-45℃)，二次预热后的原水进入内盘管蒸发器；
2)进入内盘管蒸发器的废水进行真空负压蒸发(真空度为-0.06～-0.07MPa，温度为85～90℃)，蒸发后浆液(蒸发后料浆含盐50wt％，总量约为1250kg/h)分为2部分，一部分(此部分占料浆总量的30wt％)通过循环泵进入降膜蒸发器经从第二精馏塔采出的蒸汽气相进行二次蒸发浓缩，蒸发后浓缩液返回内盘管蒸发器循环蒸发，从降膜蒸发器蒸馏出的溶剂水气相经气液分离器分离所得的液相返回内盘管蒸发器循环蒸发；另一部分(占料浆总量70wt％)作为待离心高温浆液通过循环泵进入第二换热器经初预热后原水降温后(85～90℃待离心高温浆液温度经过冷却后温度降为60℃)送入离心机(此部分通过调节阀和流量计联锁控制流量，保证每小时盐处理量为500kg/h)；
其中，从降膜蒸发器蒸馏出的溶剂水气相经气液分离器分离所得的气相与从内盘管蒸发器蒸馏出溶剂水气相合并后依次经第一精馏塔(一塔真空度为-0.09～ -0.08MPa，温度为45～50℃)，第二精馏塔(二塔真空度为-0.07～-0.06MPa，温度为75～90℃)和第三精馏塔(三塔真空度为-0.095～-0.09MPa，温度为90～ 100℃)多级精馏，得到合格溶剂(每小时回收DMF量为550kg，回收DMF溶剂各项指标如下：含量99.5wt％以上，水分小于0.2wt％，pH为4～7)；
3)经离心机分离后的母液通过输送泵返回至内盘管蒸发器循环蒸发，分离得到湿品盐经干燥，得盐成品(碳酸钾含量98wt％以上，盐产量为450kg/h)。
原水通过利用第一精馏塔蒸汽气相初预热+待离心处浆料液二次换热后再进入内盘管蒸发器，利用了第一精馏塔以及待离心浆料液自身的热量；同时降膜蒸发器利用第二精馏塔蒸汽气相作为热源加热经内盘管蒸发器蒸发后浆液，利用了第一精馏塔热量，使整个系统的余热综合利用，能耗回用率高，蒸汽可节约 30％。
蒸发在真空负压下进行的，离心除盐时通入密封氮气，保持微正压，离心机和母液槽的尾尾气接入尾气处理装置，故整个工艺中无气味逸散。
以上所述仅为本实用新型的较佳实施例而已，并不用以限制本实用新型，凡在本实用新型的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本实用新型的保护范围之内。
Claims (3)
1.一种高含盐含溶剂废水处理系统，其特征在于，包括第一换热器、第二换热器、内盘管蒸发器，降膜蒸发器，离心机，第一精馏塔、第二精馏塔和第三精馏塔，原水泵出口与第一换热器的冷媒进口相连，第一换热器的冷媒出口与第二换热器的冷媒进口相连，第二换热器的冷媒出口与内盘管蒸发器上部的进液口相连；内盘管蒸发器顶部的出气口通过气相管道与第一精馏塔进料口相连，第一精馏塔的釜底出液口与第二精馏塔的进料口相连，第二精馏塔的釜底出液口与第三精馏塔的进料口相连，第一精馏塔的蒸汽出口与第一换热器的热媒进口相连，第二精馏塔的蒸汽出口与降膜蒸发器的蒸汽进口相连；内盘管蒸发器底部的出液口通过循环泵与两路分支管相连，其中，一路分支管与降膜蒸发器的进料口相连，降膜蒸发器的出液口回连至内盘管蒸发器上部的进液口，降膜蒸发器的出气口连接有气液分离器，气液分离器的出气管并入连接内盘管蒸发器出气口与第一精馏塔进料口的气相管道，另一路分支管与第二换热器的热媒进口相连，第二换热器的热媒出口与离心机的进料口相连，离心机的出液口与母液槽的进料口相连，母液槽的出料口通过输送泵回连至内盘管蒸发器上部的进液口。
2.根据权利要求1所述的一种高含盐含溶剂废水处理系统，其特征在于，离心机和母液槽的尾气出口管与尾气吸收装置相连。
3.根据权利要求1所述的一种高含盐含溶剂废水处理系统，其特征在于，气液分离器的出液管回连至降膜蒸发器的进料口。
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