CN202610130U - 醋酸回收系统的丙酮脱除装置 - Google Patents
醋酸回收系统的丙酮脱除装置 Download PDFInfo
- Publication number
- CN202610130U CN202610130U CN 201220240220 CN201220240220U CN202610130U CN 202610130 U CN202610130 U CN 202610130U CN 201220240220 CN201220240220 CN 201220240220 CN 201220240220 U CN201220240220 U CN 201220240220U CN 202610130 U CN202610130 U CN 202610130U
- Authority
- CN
- China
- Prior art keywords
- acetone
- tower
- stripping tower
- acetic acid
- stripping
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn - After Issue
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- CSCPPACGZOOCGX-UHFFFAOYSA-N acetone Chemical compound 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CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 title claims abstract description 174
- QTBSBXVTEAMEQO-UHFFFAOYSA-N acetic acid Chemical compound 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- 238000011084 recovery Methods 0.000 title claims abstract description 18
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Abstract
本实用新型提供了一种醋酸回收系统的丙酮脱除装置，利用原有的进料槽、丙酮汽提塔和醋酸回收系统的异丙醇脱除装置，形成两次精馏脱除丙酮的装置。在进料槽和丙酮汽提塔之间，连接异丙醇汽提塔及其附属设备，异丙醇汽提塔作为丙酮第一次汽提脱除装置。异丙醇汽提塔的塔顶馏出物，先经冷凝器冷凝，再经过再冷却器冷却，送入丙酮汽提塔，丙酮汽提塔作为丙酮第二次汽提脱除装置。丙酮汽提塔的塔底流出物料经塔底冷却器冷却，送回醋酸回收装置中。本实用新型中，丙酮汽提塔进料中丙酮的浓度从4.6%左右提高到5.8%左右，送至污水处理站的废料丙酮中丙酮的浓度从80%左右，提高到90%左右。既减少精馏加热蒸汽消耗，又减少醋酸回收工艺的萃取剂消耗。
Description
醋酸回收系统的丙酮脱除装置技术领域
[0001] 本实用新型涉及化工企业排放的废水中丙酮脱除装置，尤指醋酸回收系统产生的物料流中丙酮脱除工艺装置。
背景技术
[0002] 在二醋酸纤维素等化工产品的生产线中，含有醋酸回收系统，醋酸回收系统中的稀醋酸溶液料流中往往会产生一定浓度的丙酮，由于丙酮可混溶于多种溶剂和水，将对稀醋酸的萃取过程和萃取效率产生不利影响。因此，当稀醋酸溶液中的丙酮含量过高时，就必须除去丙酮，丙酮汽提塔就是为去除溶液中的丙酮而设计的。但是，传统的丙酮汽提塔处理后的塔顶流出物料(塔顶馏出物)中的丙酮浓度也只有35%-80%左右，脱除丙酮不够彻底，而且会带走部分己烷等有用的萃取剂原料。
[0003] 另外，当醋酸回收系统中的异丙醇含量过高时，也必须将其除去。如不除去，会影 响设备的运行周期。异丙醇汽提塔是为去除溶液中的异丙醇而设计的。异丙醇汽提塔和丙酮汽提塔都属于精馏塔，但异丙醇汽提塔工作时塔顶部和塔底部的温度均高于丙酮汽提塔的相应部位的温度。而且，异丙醇汽提塔脱除的异丙醇，存在于塔底产品；丙酮汽提塔脱除的丙酮，存在于塔顶产品。
[0004] 专利申请号为201110006970.9的说明书中公开的一种“减压汽提式精馏回收稀丙酮水溶液中丙酮的方法”，公开了减压汽提式精馏回收稀丙酮水溶液中丙酮的方法。该方法将含有丙酮的稀溶液通过换热器与精馏塔中塔釜排放出来的高温釜液进行换热，达到85-95°C后，从精馏塔8#-16#塔板之间进入精馏塔中；塔顶操作压强为O. 07-0. 09MPa ；塔釜操作压强为O. 120-0. 130MPa ;精馏塔的塔顶馏出物经冷凝器冷却到40-55°C后，部分馏出物作为丙酮产品采出，部分馏出物作为回流，控制回流质量与产品质量的回流比为O. 5-6. 6 ： I。该实用新型减少了用于冷凝塔顶蒸汽的冷却水的用量和用于加热的塔底蒸汽的用量，虽可以降低精馏操作费用，但是对于丙酮的提纯浓度和提纯效率并未有大的改进。
[0005] 2000年第二期《化工进展》刊登的《丙酮汽提塔系统的工艺改造》一文，保留原丙酮汽提塔，从流出液塔塔顶出料管线上接一管线到丙酮汽提塔作为丙酮汽提塔的进料，将丙酮塔塔底出料接至主蒸馏塔的分层器重相侧。该改造设备工作稳定，脱除丙酮的效率提高。本实用新型在此工艺路线的基础上，将其与醋酸回收系统的异丙醇脱除装置重新组合，形成脱除丙酮的两次精馏工艺路线，进一步提高了脱除丙酮的效率。既减少精馏加热蒸汽消耗，又减少醋酸回收工艺的萃取剂消耗。
发明内容
[0006] 实用新型目的：减少丙酮脱除精馏过程的加热蒸汽的消耗，减少醋酸回收工艺的萃取剂消耗，，提供一种采用不同的汽提塔份分两次脱除的丙酮脱除装置。
[0007] 技术方案：本实用新型提供的一种醋酸回收系统流出稀醋酸溶液物料中丙酮脱除装置，在醋酸回收装置之外，包括进料槽、丙酮汽提塔、冷凝器B、污水处理站、再沸塔B、塔底冷却器B，还包括异丙醇汽提塔、冷凝器A、回流罐、再沸塔A、塔底冷却器A。在进料槽和丙酮汽提塔之间连接有异丙醇汽提塔，异丙醇汽提塔作为丙酮脱除的第一次汽提装置(采用异丙醇汽提塔的设备和汽提工艺)，丙酮汽提塔作为丙酮的第二次汽提装置(采用丙酮汽提塔的设备和汽提工艺)。
[0008] 所述的异丙醇汽提塔的塔顶连接有冷凝器A，再连接有回流罐，然后再连接到丙酮汽提塔的入口。丙酮汽提塔的塔顶连接有冷凝器B，冷凝器B后有支管路连接至污水处理站，另有支管路其余连接回丙酮汽提塔的塔顶。丙酮汽提塔的塔底连接有再沸塔B、塔底冷却器B，塔底冷却器B后或有管路连接醋酸回收装置。
[0009] 所述的异丙醇汽提塔的塔底依次可以连接有再沸塔A，还可以连接有塔底冷却器A，其塔底流出物料经塔底冷却器A冷却后有管路连接醋酸回收装置，塔底流出物料循环使用，节约成本，减少排放。
[0010] 在所述的冷凝器A和回流罐之间最好连接有再冷却器，将冷凝液化的塔顶流出物 料进一步冷却，以便部分回流时不影响汽提塔中物料的温度稳定性，以及便于部分采出的后续处理利用。
[0011] 有益效果：本实用新型的装置中，丙酮汽提塔的入口流进物料中丙酮的浓度从原来4. 2%左右提高到5. 34%左右，送至污水处理站的流出物料中丙酮的浓度从原来80%左右提高到90%左右，甚至达到95%。塔顶馏出物中丙酮的浓度提高后，既减少丙酮第二次汽提过程的加热蒸汽的消耗，又减少醋酸回收工艺的己烷等萃取剂的消耗，节约生产成本。而且，利用了异丙醇汽提塔分离异丙醇(在塔底流出物料中）的工艺副产品（塔顶馏出物)，延长了丙酮汽提塔的运行周期。
附图说明
[0012] 附图是本实用新型的一个结构和工艺流程示意图；
[0013] 图中：1、醋酸回收装置；2、再沸塔A ;3、进料槽；4、异丙醇汽提塔；5、冷凝器A ;6、再冷却器；7、回流罐；8、丙酮汽提塔；9、冷凝器B ;10、污水处理站；12、塔底冷却器B ;13、再沸塔B ; 14、塔底冷却器A。
具体实施方式实施例
[0014] 选取如附图中所示的各种部件，将各个部件用相应的管路连接起来，形成一个醋酸回收系统流出物料中丙酮脱除装置。该装置中包括醋酸回收装置1，在进料槽3和丙酮汽提塔8之间连接有异丙醇汽提塔4。所述的异丙醇汽提塔4的塔顶连接有冷凝器A5、再冷却器6，再连接有回流罐7，然后连接到丙酮汽提塔8的入口 ；丙酮汽提塔8的塔顶连接有冷凝器B9，再连接到污水处理站10 ;丙酮汽提塔8的塔底连接有再沸塔B13，再连接有塔底冷却器B12。
[0015] 附图所示的醋酸回收系统废水中丙酮脱除装置，在实际生产中采用的脱除工艺具有下述工艺步骤：[0016] I)醋酸回收系统流出物料进入异丙醇汽提塔4的入口，采用异丙醇汽提塔4进行第一次汽提过程；
[0017] 2)异丙醇汽提塔4的塔顶流出物料，经过冷凝器A5冷凝后，再经过再冷却器6深度冷却，降温至常温，流进回流罐7，再送入丙酮汽提塔8的入口，采用丙酮汽提塔8进行第二次汽提过程；
[0018] 3)丙酮汽提塔8的塔顶流出物料经过冷凝器B9冷凝后，送至污水处理站10 ;丙酮汽提塔8的塔底流出物料经过再沸塔B13的循环加热回流利用后，再经过塔底冷却器B14的冷却处理；
[0019] 4)异丙醇汽提塔4的塔底流出物料经过再沸塔A2的循环利用后，再经过塔底冷却器A冷却处理后，送回醋酸回收装置I中。
Claims (3)
1. ー种醋酸回收系统的丙酮脱除装置，包括进料槽（3)、丙酮汽提塔（8)、冷凝器B(9)、污水处理站（10)、再沸塔B( 13)、塔底冷却器B( 12)，其特征在于：还包括异丙醇汽提塔（4)、冷凝器A (5)、回流罐（7)、再沸塔A (2)、塔底冷却器A (14);在进料槽（3)和丙酮汽提塔(8)之间连接有异丙醇汽提塔（4)，异丙醇汽提塔（4)作为丙酮脱除的第一次汽提装置，丙酮汽提塔（8)作为丙酮的第二次汽提装置； 所述的异丙醇汽提塔（4)的塔顶连接有冷凝器A (5)，再连接有回流罐（7)，然后再连接到丙酮汽提塔（8)的入口 ；丙酮汽提塔（8)的塔顶连接有冷凝器B (9)，冷凝器B (9)后有支管路连接至污水处理站（10)，另有支管路连接回丙酮汽提塔（8)的塔顶；丙酮汽提塔（8)的塔底连接有再沸塔B (13)、塔底冷却器B (12)，塔底冷却器（12)后或有管路连接醋酸回收装置（I)。
2.如权利要求I所述的醋酸回收系统的丙酮脱除装置，其特征在于：所述的异丙醇汽提塔（4)的塔底依次连接有再沸塔A (2)、塔底冷却器A (14)，其塔底流出物料经塔底冷却器A (14)冷却后有管路连接醋酸回收装置（I)。
3.如权利要求I所述的醋酸回收系统的丙酮脱除装置，其特征在于：在所述的冷凝器A (5)和回流罐（7)之间连接有再冷却器（6)。
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