CN204261367U - 一种mvr蒸发装置 - Google Patents
一种mvr蒸发装置 Download PDFInfo
- Publication number
- CN204261367U CN204261367U CN201420660636.4U CN201420660636U CN204261367U CN 204261367 U CN204261367 U CN 204261367U CN 201420660636 U CN201420660636 U CN 201420660636U CN 204261367 U CN204261367 U CN 204261367U
- Authority
- CN
- China
- Prior art keywords
- compressor
- indirect steam
- evaporator
- outlet
- preevaporator
- 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- Withdrawn - After Issue
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- 239000007788 liquid Substances 0.000 claims abstract description 27
- 238000001640 fractional crystallisation Methods 0.000 claims abstract description 20
- 238000001704 evaporation Methods 0.000 claims abstract description 18
- 239000011552 falling film Substances 0.000 claims description 14
- 239000012141 concentrate Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 6
- 238000004094 preconcentration Methods 0.000 abstract description 5
- 238000009835 boiling Methods 0.000 abstract description 3
- 238000007906 compression Methods 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 12
- 238000002425 crystallisation Methods 0.000 description 8
- 230000005712 crystallization Effects 0.000 description 8
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- WCUXLLCKKVVCTQ-UHFFFAOYSA-M potassium chloride Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nODVweCcgaGVpZ2h0PSc4NXB4JyB2aWV3Qm94PScwIDAgODUgODUnPgo8IS0tIEVORCBPRiBIRUFERVIgLS0+CjxyZWN0IHN0eWxlPSdvcGFjaXR5OjEuMDtmaWxsOiNGRkZGRkY7c3Ryb2tlOm5vbmUnIHdpZHRoPSc4NS4wJyBoZWlnaHQ9Jzg1LjAnIHg9JzAuMCcgeT0nMC4wJz4gPC9yZWN0Pgo8dGV4dCB4PSc1LjEnIHk9JzUzLjYnIGNsYXNzPSdhdG9tLTAnIHN0eWxlPSdmb250LXNpemU6MjNweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjt0ZXh0LWFuY2hvcjpzdGFydDtmaWxsOiM1QkI3NzInID5DPC90ZXh0Pgo8dGV4dCB4PScyMS4xJyB5PSc1My42JyBjbGFzcz0nYXRvbS0wJyBzdHlsZT0nZm9udC1zaXplOjIzcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojNUJCNzcyJyA+bDwvdGV4dD4KPHRleHQgeD0nMjYuMCcgeT0nNDQuMycgY2xhc3M9J2F0b20tMCcgc3R5bGU9J2ZvbnQtc2l6ZToxNXB4O2ZvbnQtc3R5bGU6bm9ybWFsO2ZvbnQtd2VpZ2h0Om5vcm1hbDtmaWxsLW9wYWNpdHk6MTtzdHJva2U6bm9uZTtmb250LWZhbWlseTpzYW5zLXNlcmlmO3RleHQtYW5jaG9yOnN0YXJ0O2ZpbGw6IzVCQjc3MicgPi08L3RleHQ+Cjx0ZXh0IHg9JzU0LjknIHk9JzUzLjYnIGNsYXNzPSdhdG9tLTEnIHN0eWxlPSdmb250LXNpemU6MjNweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjt0ZXh0LWFuY2hvcjpzdGFydDtmaWxsOiMzQjQxNDMnID5LPC90ZXh0Pgo8dGV4dCB4PSc3MC45JyB5PSc0NC4zJyBjbGFzcz0nYXRvbS0xJyBzdHlsZT0nZm9udC1zaXplOjE1cHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojM0I0MTQzJyA+KzwvdGV4dD4KPC9zdmc+Cg== [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 4
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- 239000000463 material Substances 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances 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[NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- 235000019270 ammonium chloride Nutrition 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
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Abstract
本实用新型涉及一种MVR蒸发装置，包括预蒸发器、蒸发结晶器、第一压缩机和第二压缩机，所述第一压缩机的进、出口分别连接预蒸发器的二次蒸汽出口和入口，所述第二压缩机位于蒸发结晶器的二次蒸汽回路上。由于分离结晶器的浓缩浓度高，二次蒸汽经压缩后要求达到的温升相对也高，本实用新型的二次蒸汽经过分压，使进入分离结晶器的二次蒸汽单独由第二压缩机进行压缩，其单独进入第二压缩机，而预浓缩的二次蒸汽由第一压缩机压缩升温，相对于蒸汽全压进入一台压缩机，大大降低了对压缩机的流量和温升要求，从而达到降低成本和运行耗能的目的。本实用新型适用于可以用于大蒸发量、高沸点料液的浓缩蒸发。
Description
技术领域
[0001] 本实用新型涉及液体浓缩领域，特别是一种MVR蒸发装置。
背景技术
[0002] MVRCMechanical Vapor Recompress1n机械蒸汽再压缩)工作原理是通过机械驱动的压缩机将蒸发器蒸出的低压低温的蒸汽，压缩至较高压力与温度，成为高温位的蒸汽，作为加热器、再沸器和蒸发器热源，即回收了二次蒸汽汽化潜热，从而节约了能耗。但是，对于蒸发结晶装置，蒸发量越大且料液沸点升高越大的，对压缩机的负荷要求就越高，其成本与耗能也就急剧上升。
[0003] 现有技术中，蒸发结晶蒸发量大且沸点升高大的料液时，如低浓度氯化铵废水，其MVR蒸发结晶系统通常先进行预蒸发提高浓度，再蒸发结晶从而进一步提高浓度，MVR单元采用两级压缩机全压串联的方式，对来自预蒸发和蒸发结晶的二次蒸汽进行压缩，压缩机承载了整个蒸发系统的大蒸发量，再加上对压缩机的高温升要求，从而导致了蒸发结晶的高成本和高耗能。
实用新型内容
[0004] 为了克服上述技术问题，本实用新型的目的在于提供一种节约成本、降低能耗的MVR蒸发装置。
[0005] 本实用新型所采用的技术方案是:
[0006] 一种MVR蒸发装置，包括预蒸发器、蒸发结晶器、第一压缩机和第二压缩机，所述第一压缩机的进、出口分别连接预蒸发器的二次蒸汽出口和入口，所述第二压缩机位于蒸发结晶器的二次蒸汽回路上。
[0007] 作为上述技术方案的进一步改进，所述第二压缩机的进、出口分别连接蒸发结晶器的二次蒸汽出口和入口。
[0008] 作为上述技术方案的进一步改进，所述蒸发结晶器的二次蒸汽出口连接第一压缩机的入口，所述第二压缩机的进口连接第一压缩机的出口，所述第二压缩机的出口连接蒸发结晶器的二次蒸汽入口。
[0009] 作为上述技术方案的进一步改进，所述预蒸发器的浓缩液循环管路上设有循环泵，所述蒸发结晶器的进液口通过管道连接循环泵的出口。
[0010] 作为上述技术方案的进一步改进，所述蒸发结晶器为强制循环蒸发结晶器，包括换热器、分离结晶器和强制循环泵，所述换热器的进液口作为蒸发结晶器的进液口，所述换热器的出液口与分离结晶器的进液口通过管道相连，所述强制循环泵位于换热器的进液口和分离结晶器的出液口之间，所述蒸发结晶器的二次蒸汽出口在分离结晶器顶部，入口在换热器上。
[0011] 作为上述技术方案的进一步改进，所述预蒸发器为降膜蒸发器，包括蒸发器本体、与蒸发器本体相连的气液分离室，所述第一压缩机连接气液分离室和蒸发器本体，所述蒸发器本体顶部的循环液进口和底部的循环液出口之间通过管道和循环泵相连，构成预蒸发器的浓缩液循环管路。
[0012] 本实用新型的有益效果是:由于分离结晶器的浓缩浓度高，二次蒸汽经压缩后要求达到的温升相对也高，本实用新型的二次蒸汽经过分压，使进入分离结晶器的二次蒸汽单独由第二压缩机进行压缩，其单独进入第二压缩机，而预浓缩的二次蒸汽由第一压缩机压缩升温，相对于蒸汽全压进入一台压缩机，大大降低了对压缩机的流量和温升要求，从而达到降低成本和运行耗能的目的。
附图说明
[0013] 下面结合附图和实施方式对本实用新型进一步说明。
[0014] 图1是本实用新型第一实施例的示意图；
[0015] 图2是本实用新型第二实施例的示意图。
具体实施方式
[0016] 如图1和图2所示的MVR蒸发装置，包括预蒸发器、蒸发结晶器、第一压缩机I和第二压缩机2，第一压缩机I的进、出口分别连接预蒸发器的二次蒸汽出口和入口，第二压缩机2位于蒸发结晶器的二次蒸汽回路上。
[0017] 预蒸发器为降膜蒸发器6，包括蒸发器本体61、与蒸发器本体61相连的气液分离室62，第一压缩机I连接气液分离室62和蒸发器本体61的顶部，将气液分离室62分离的二次蒸汽压缩升温后返回蒸发器本体61内加热。蒸发器本体61顶部的循环液进口和底部的循环液出口之间通过管道和循环泵3相连，构成降膜蒸发器6的浓缩液循环管路。在达到下一步工艺的浓度前，浓缩液经过循环泵3的循环作用，在降膜蒸发器6内保持循环和不断浓缩。
[0018] 蒸发结晶器为强制循环蒸发结晶器4，包括换热器42、分离结晶器41和强制循环泵5。换热器42的进液口为强制循环蒸发结晶器4的进液口，换热器42的出液口与分离结晶器41的进液口通过管道相连。强制循环泵5位于换热器42的进液口和分离结晶器41的出液口之间，同时强制循环泵5的入口通过管道连接循环泵3的出口，达到预浓缩浓度的浓缩液可以通过循环泵3和强制循环泵5进入换热器42内。蒸发结晶器的二次蒸汽出口在分离结晶器41顶部，入口在换热器42上并连接第二压缩机2的出口。
[0019] 如图1所示的第一实施例中，第一压缩机I的进、出口通过管道直接连接降膜蒸发器6的二次蒸汽出口和入口，第二压缩机2的进、出口分别连接强制循环蒸发结晶器4的二次蒸汽出口和入口，两台压缩机相互分隔互不关联，单独供热。
[0020] 该实施例中的分压蒸发方法如下:
[0021] a.原料液进入降膜蒸发器6进行预蒸发，料液通过其下部的出口经循环泵3输送回顶部再次进入降膜蒸发器6进行蒸发；料液浓度和温度达到动态平衡后，循环泵3输送部分料液继续循环蒸发，其它部分输送到强制循环泵5的进料管道。
[0022] b.强制循环泵5将料液输送到换热器42进行换热，换热后料液进入分离结晶器41进行闪蒸；分离结晶器41中的晶浆从其下部进入强制循环泵5的进料管道继续循环；晶浆达到设定要求后从下部出料管道流向后续工艺。
[0023] c.降膜蒸发器6的冷凝水和强制循环换热器42的冷暖水进入冷凝水罐7，冷凝水经冷凝水泵8排出或流向后续工艺。
[0024] 上述步骤a中，预浓缩产生的二次蒸汽全部经第一压缩机I压缩升温后进入降膜蒸发器6作为热源换热，步骤b中强制循环蒸发结晶器4浓缩结晶产生二次蒸汽单独经第二压缩机2压缩升温后返回强制循环蒸发结晶器4进行换热。
[0025] 如图2所示的第二实施例中，蒸发结晶器的二次蒸汽出口连接第一压缩机I的入口，第二压缩机2的进口连接第一压缩机I的出口，第二压缩机2的出口连接蒸发结晶器的二次蒸汽入口。
[0026] 该实施例中的分压蒸发方法如下:
[0027] a.原料液进入降膜蒸发器6进行预蒸发，料液通过其下部的出口经循环泵3输送回顶部再次进入降膜蒸发器6进行蒸发；料液浓度和温度达到动态平衡后，循环泵3输送部分料液继续循环蒸发，其它部分输送到强制循环泵5的进料管道。
[0028] b.强制循环泵5将料液输送到换热器42进行换热，换热后料液进入分离结晶器41进行闪蒸；分离结晶器41中的晶浆从其下部进入强制循环泵5的进料管道继续循环；晶浆达到设定要求后从下部出料管道流向后续工艺。
[0029] c.降膜蒸发器6的冷凝水和强制循环换热器42的冷暖水进入冷凝水罐7，冷凝水经冷凝水泵排出或流向后续工艺。
[0030] 上述步骤a和b中，预浓缩以及浓缩结晶中产生的二次蒸汽先同时经第一压缩机I压缩升温后，一部分进入降膜蒸发器6作为热源换热，另外一部分由第二压缩机2再次压缩升温，并进入强制循环蒸发结晶器4进行换热。
[0031] 上述实施例中的装置和方法适用于可以用于氯化铵(NH4Cl)蒸发结晶工艺，也可以用于氯化钠(NaCl)和氯化钾(KCl)等物质的蒸发结晶工艺。
[0032] 以上实施例仅用以说明本实用新型的技术方案而非限制，尽管参照较佳实施例对本实用新型进行了详细说明，本领域的普通技术人员应当理解，可以对本实用新型的技术方案进行修改或者等同替换，而不脱离本实用新型技术方案的宗旨和范围，其均应涵盖在本实用新型的权利要求范围当中。
Claims (6)
1.一种MVR蒸发装置，其特征在于:包括预蒸发器、蒸发结晶器、第一压缩机和第二压缩机，所述第一压缩机的进、出口分别连接预蒸发器的二次蒸汽出口和入口，所述第二压缩机位于蒸发结晶器的二次蒸汽回路上。
2.根据权利要求1所述的MVR蒸发装置，其特征在于:所述第二压缩机的进、出口分别连接蒸发结晶器的二次蒸汽出口和入口。
3.根据权利要求1所述的MVR蒸发装置，其特征在于:所述蒸发结晶器的二次蒸汽出口连接第一压缩机的入口，所述第二压缩机的进口连接第一压缩机的出口，所述第二压缩机的出口连接蒸发结晶器的二次蒸汽入口。
4.根据权利要求1或2或3所述的MVR蒸发装置，其特征在于:所述预蒸发器的浓缩液循环管路上设有循环泵，所述蒸发结晶器的进液口通过管道连接循环泵的出口。
5.根据权利要求4所述的MVR蒸发装置，其特征在于:所述蒸发结晶器为强制循环蒸发结晶器，包括换热器、分离结晶器和强制循环泵，所述换热器的进液口作为蒸发结晶器的进液口，所述换热器的出液口与分离结晶器的进液口通过管道相连，所述强制循环泵位于换热器的进液口和分离结晶器的出液口之间，所述蒸发结晶器的二次蒸汽出口在分离结晶器顶部，入口在换热器上。
6.根据权利要求4所述的MVR蒸发装置，其特征在于:所述预蒸发器为降膜蒸发器，包括蒸发器本体、与蒸发器本体相连的气液分离室，所述第一压缩机连接气液分离室和蒸发器本体，所述蒸发器本体顶部的循环液进口和底部的循环液出口之间通过管道和循环泵相连，构成预蒸发器的浓缩液循环管路。
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104399266A (zh) * | 2014-11-05 | 2015-03-11 | 广州市心德实业有限公司 | 一种mvr蒸发装置及分压蒸发方法 |
| CN105540626A (zh) * | 2015-12-18 | 2016-05-04 | 苏州中色德源环保科技有限公司 | 氧化铝母液mvr循环蒸发装置及工艺 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104399266A (zh) * | 2014-11-05 | 2015-03-11 | 广州市心德实业有限公司 | 一种mvr蒸发装置及分压蒸发方法 |
| CN104399266B (zh) * | 2014-11-05 | 2016-08-31 | 广州市心德实业有限公司 | 一种mvr蒸发装置及分压蒸发方法 |
| CN105540626A (zh) * | 2015-12-18 | 2016-05-04 | 苏州中色德源环保科技有限公司 | 氧化铝母液mvr循环蒸发装置及工艺 |
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