CN209809543U - 七效管式降膜蒸发器组 - Google Patents
七效管式降膜蒸发器组 Download PDFInfo
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- CN209809543U CN209809543U CN201920045343.8U CN201920045343U CN209809543U CN 209809543 U CN209809543 U CN 209809543U CN 201920045343 U CN201920045343 U CN 201920045343U CN 209809543 U CN209809543 U CN 209809543U
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- 239000011552 falling film Substances 0.000 title claims abstract description 33
- 230000000694 effects Effects 0.000 claims abstract description 140
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- 239000007789 gas Substances 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N AI2O3 Inorganic materials 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[O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000003379 elimination reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 229910052782 aluminium Inorganic materials 0.000 description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminum Chemical compound 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[Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 238000004090 dissolution Methods 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 2
- 238000006011 modification reaction Methods 0.000 description 2
- 239000010413 mother solution Substances 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound 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[Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- WNROFYMDJYEPJX-UHFFFAOYSA-K Aluminium hydroxide Chemical compound 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- 238000002156 mixing Methods 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound 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Abstract
本实用新型涉及到一种七效管式降膜蒸发器组，该七效管式降膜蒸发器组主要包括Ⅰ效蒸发器～Ⅶ效蒸发器以及第一～第四自蒸发器、Ⅰ～Ⅱ效预热器、原液闪蒸器、各效冷凝水罐等，本实用新型通过对原液分段浓缩、对各效蒸发器生成的二次蒸汽、各效冷凝水进行闪蒸生产的二次蒸汽、强制循环排盐蒸发器产生的二次蒸汽、各自蒸发器产生的次蒸汽进行充分的利用，大大提高了整个蒸发浓缩工艺的蒸发效率。
Description
技术领域：
本实用新型涉及一种七效管式降膜蒸发器组。
背景技术：
在当代国民经济中，铝的应用几乎是无处不在，铝已经成为仅次于钢铁的最重要的金属材料。金属铝是以氧化铝为原料，通过电解熔融的氧化铝而制取的。全世界氧化铝产量的90％以上为冶金级氧化铝，用于电解制取金属铝。
拜耳法生产氧化铝工艺流程主要工序包括：原矿浆制备、高压溶出、晶种分解、母液蒸发、氢氧化铝焙烧等，最重要的的是高压溶出和母液蒸发，行业内有一个普遍的说法：蒸发是龙头，溶出是心脏。
七效管式降膜蒸发器组用于母液蒸发具有高效、节能降耗的显著特点，符合《国家重点支持的高新技术领域》政策要求，在能源高效利用方面具有明显的优势，但目前的种分母液七效蒸发浓缩工艺及七效管式降膜蒸发器组的汽耗比、二次蒸汽冷凝水含碱量均比较高，以 400T/h七效管式降膜蒸发器组为例，其采用现有的种分母液七效蒸发浓缩工艺进行蒸发浓缩时，原液进料流量约1000m3/h，蒸水量在350～370T/h，蒸发汽耗比≥0.2吨.汽/吨.水，二次蒸汽冷凝水含碱量≥30mg/L，汽耗比高则会增加生产成本，二次蒸汽冷凝水含碱量高则会提高企业水处理成本和种分母液的碱流失。
实用新型内容：
本实用新型要解决的技术问题是：提供一种蒸发效率更高、汽耗比更低的七效管式降膜蒸发器组。
为解决上述技术问题，本实用新型所采用的技术方案是：一种七效管式降膜蒸发器组，用于实施上述七效蒸发浓缩工艺，包括Ⅰ效蒸发器～Ⅶ效蒸发器，其特征在于，还包括原液闪蒸器、第一自蒸发器～第四自蒸发器、Ⅰ效预热器、Ⅱ效预热器以及强制循环排盐蒸发器，其中，Ⅴ效蒸发器、Ⅳ效蒸发器、Ⅲ效蒸发器、Ⅱ效预热器、Ⅱ效蒸发器、Ⅰ效预热器、Ⅰ效蒸发器、第一自蒸发器～第四自蒸发器依次联接形成第一段溶液浓缩回路；原液闪蒸器、Ⅶ效蒸发器、Ⅵ效蒸发器依次联接形成第二段溶液浓缩回路；经第一段溶液浓缩回路浓缩后的部分溶液分流进入强制循环排盐蒸发器形成第三段溶液浓缩回路；
各效蒸发器分离室的二次蒸汽出口与下一效蒸发器的加热室蒸汽进口连通，Ⅰ效蒸发器的蒸汽进口与新蒸汽管道连通，Ⅶ效蒸发器的二次蒸汽出口与水冷器连通；
强制循环排盐蒸发器加热室的蒸汽进口与新蒸汽管道连通，强制循环排盐蒸发器分离室的二次蒸汽出口与Ⅵ效蒸发器的加热室蒸汽进口连通；
第一级自蒸发器的二次蒸汽出口与Ⅱ效预热器连通，第二～第四级自蒸发器的二次蒸汽出口分别与Ⅳ～Ⅵ效蒸发器加热室蒸汽进口连通；
原液闪蒸器的二次蒸汽出口与Ⅶ效蒸发器加热室蒸汽进口连通；
所述Ⅰ效蒸发器上依次连接有Ⅰ效-1#～Ⅰ效-n#(n≤7)冷凝水罐，Ⅰ效-n#冷凝水罐通过一次冷凝水泵连接一次冷凝水槽；Ⅰ效-1#～Ⅰ效-n#(n≤7)冷凝水罐上分别设置有二次蒸汽出口，Ⅰ效-1#～Ⅰ效-n#(n≤7)冷凝水罐的二次蒸汽出口分别连接1～N(N≤Ⅶ)效蒸发器加热室蒸汽进口；
所述Ⅱ效蒸发器～Ⅶ效蒸发器上分别对应连接有Ⅱ效冷凝水罐～Ⅶ效冷凝水罐，Ⅱ效冷凝水罐～Ⅶ效冷凝水罐依次串联，Ⅱ效冷凝水罐～Ⅶ效冷凝水罐上端均开设有蒸汽出口，Ⅱ效冷凝水罐～Ⅶ效冷凝水罐的蒸汽出口一一对应地连通到Ⅱ效蒸发器～Ⅶ效蒸发器加热室的蒸汽进口，Ⅶ效冷凝水罐通过二次冷凝水泵连接二次冷凝水槽。
作为一种优选方案，Ⅰ～Ⅶ效蒸发器上盖顶部均设置了排不凝气系统，以及时排出混入水蒸气的少量空气和其它不凝性气体。
作为一种优选方案，Ⅰ～Ⅶ效蒸发器各自的分离室与加热室通过循环管路连通，循环管路上设置有循环泵，上述各效蒸发器分离室的出料口通过过料泵连接到上一效蒸发器的循环泵进料口，其中Ⅲ效过料泵和Ⅱ效循环泵之间设有Ⅱ效预热器，Ⅱ效过料泵和Ⅰ效循环泵之间设有Ⅰ效预热器；Ⅵ效、Ⅶ效蒸发器各自的分离室与加热室通过循环管路连通，循环管路上设置有循环泵，Ⅶ效蒸发器分离室的出料口通过过料泵连接到Ⅵ效蒸发器的循环泵进料口；强制循环排盐蒸发器的进料口通过强制循环进料泵与第四自蒸发器的出料口连通，强制循环排盐蒸发器的分离室和加热室通过循环管路连通，循环管路上设置有强制循环泵，强制循环排盐蒸发器的出料口通过强制循环出料泵与盐沉降槽连通。
作为一种优选方案，Ⅰ～Ⅶ效蒸发器均为分体式，分别包括上下设置且相互连接的Ⅰ～Ⅶ效管式降膜加热室和Ⅰ～Ⅶ效集液室、并排设置在Ⅰ～Ⅶ效集液室一侧的Ⅰ～Ⅶ效分离室，Ⅰ～Ⅶ效集液室和Ⅰ～Ⅶ效分离室一一对应地通过各连通管连接。
作为一种优选方案，Ⅰ～Ⅶ效集液室、Ⅰ～Ⅶ效分离室的底部均成锥形，第一～第四自蒸发器的底部也成锥形。
作为一种优选方案，Ⅱ效蒸发器的加热室蒸汽进口通过第一截止阀与新蒸汽管道连通，Ⅱ效蒸发器的加热室蒸汽进口通过第二截止阀与Ⅰ效蒸发器的分离室二次蒸汽出口连通，Ⅱ效蒸发器的分离室出料口通过第三截止阀与第一自蒸发器连通，Ⅱ效蒸发器的分离室出料口通过第四截止阀与Ⅰ效预热器连通，所述Ⅰ效蒸发器的分离室出料口通过第五截止阀与第一自蒸发器连通。
本实用新型的有益效果是：由于本实用新型所述七效管式降膜蒸发器组将Ⅰ～Ⅶ效蒸发器分配成两段溶液浓缩回路，缩短溶液浓缩回路的路径，提高浓缩效率，其中一段通过原液闪蒸器初步闪蒸提高溶液浓度，然后再进入负压工况的Ⅶ效蒸发器、Ⅵ效蒸发器进一步浓缩，提高该段溶液浓缩回路的浓缩效率，最终使整个七效管式降膜蒸发器组的蒸发效率得到大幅提升，并采用强制循环排盐蒸发器对溶液进行排盐，控制溶液中杂质浓度。
同时，通过优化设计的蒸汽回路，充分利用Ⅰ～Ⅶ效蒸发器的分离室、各效冷凝水罐、第一～第四自蒸发器、以及原液闪蒸器、强制循环排盐蒸发器的分离室生成的二次蒸汽热能，对溶液进行加热，有效降低了蒸汽能耗。
进一步通过对进入Ⅱ效蒸发器和Ⅰ效蒸发器的溶液进行预热，提高进入Ⅱ效蒸发器和Ⅰ效蒸发器的溶液温度达到或接近本效溶液沸点，提高溶液在Ⅰ效蒸发器加热室和Ⅱ效蒸发器加热室内的膜式传热效率，最终提高Ⅰ效蒸发器和Ⅱ效蒸发器的蒸发效率。
附图说明：
下面结合附图对本实用新型的具体实施方式作进一步详细说明，其中：
图1是本实用新型所述七效管式降膜蒸发器组的结构示意图；
图2是本实用新型所述Ⅰ效蒸发器的结构示意图；
图3是本实用新型所述Ⅰ效蒸发器和Ⅱ效蒸发器的具体连接结构示意图；
图4是本实用新型所述工艺的溶液浓缩流程图；
图5是本实用新型所述工艺的蒸汽利用流程图；
图6是本实用新型所述工艺的冷凝水热能利用流程图。
图1～图3中：1、Ⅰ效蒸发器，1-1、Ⅰ效管式降膜加热器，1-2、Ⅰ效集液室，1-3、Ⅰ效分离室，1-4、连通管，2、Ⅱ效蒸发器，3、Ⅲ效蒸发器，4、Ⅳ效蒸发器，5、Ⅴ效蒸发器， 6、Ⅵ效蒸发器，7、Ⅶ效蒸发器，8、原液闪蒸器，9、第一自蒸发器，10、第二自蒸发器， 11、第三自蒸发器，12、第四自蒸发器，13、Ⅰ效预热器，14、Ⅱ效预热器，15、强制循环排盐蒸发器，16、母液出料泵，17、原液进料泵，18、排不凝气系统，19、水冷器，20-1、Ⅰ效-1#冷凝水罐，20-2、Ⅰ效-2#冷凝水罐，20-3、Ⅰ效-3#冷凝水罐，20-4、Ⅰ效-4#冷凝水罐，20-5、Ⅰ效-5#冷凝水罐，21、一次冷凝水泵，22、Ⅱ效冷凝水罐，23、Ⅲ效冷凝水罐， 24、Ⅳ效冷凝水罐，25、Ⅴ效冷凝水罐，26、Ⅵ效冷凝水罐，27、Ⅶ效冷凝水罐，28、二次冷凝水泵，29、循环泵，30、过料泵，31、强制循环进料泵，32、强制循环泵，33、强制循环出料泵，34、第一截止阀，35、新蒸汽管道，36、第二截止阀，37、第三截止阀，38、第四截止阀，39、第五截止阀，40、强制效冷凝水罐。
具体实施方式：
下面结合附图，详细描述本实用新型的具体实施方案。
如图1～图3是一种七效管式降膜蒸发器组，用于实施上述七效蒸发浓缩工艺，如图1所示，七效管式降膜蒸发器组包括Ⅰ效蒸发器1～Ⅶ效蒸发器7，还包括原液闪蒸器8、第一自蒸发器9～第四自蒸发器12、Ⅰ效预热器13、Ⅱ效预热器14以及强制循环排盐蒸发器15，其中，Ⅴ效蒸发器5、Ⅳ效蒸发器4、Ⅲ效蒸发器3、Ⅱ效预热器14、Ⅱ效蒸发器2、Ⅰ效预热器13、Ⅰ效蒸发器1、第一自蒸发器9～第四自蒸发器12依次联接形成第一段溶液浓缩回路；原液闪蒸器8、Ⅶ效蒸发器7、Ⅵ效蒸发器6依次联接形成第二段溶液浓缩回路；经第一段溶液浓缩回路浓缩后的部分溶液分流进入强制循环排盐蒸发器15形成第三段溶液浓缩回路；
第一段溶液浓缩回路与第二段溶液浓缩回路用于蒸发浓缩溶液以得到浓度符合要求的母液，分成两段浓缩提高浓缩效率、降低能耗，第三段溶液浓缩回路用于控制母液中的杂质浓度，确保母液质量。
第一段溶液浓缩回路中的第一自蒸发器9～第四自蒸发器12可在不需要外部提供热量的情况下，利用溶液自身具备的高温、高压力条件，进行扩容蒸发，从溶液里闪蒸出部分二次蒸汽，同时溶液的温度、压力降低，浓度增高。第一自蒸发器9～第四自蒸发器12内可分别设置有除沫器，对二次蒸汽进行汽液分离，去除带碱液滴，使排出的二次蒸汽更洁净。
溶液在第一自蒸发器9～第四自蒸发器12内“闪蒸”过程中同时进行循环流动，使闪蒸进行的更完全。
第二段溶液浓缩回路中，原液闪蒸器8可有效降低溶液温度，提高溶液浓度，使溶液温度与Ⅶ效蒸发器7内溶液温度差缩小，降低溶液进入Ⅶ效蒸发器7时的闪蒸剧烈程度，降低Ⅶ效蒸发器7分离室内除沫器(图中未示出)的工作负荷，大大降低从Ⅶ效蒸发器7分离室排出的二次蒸汽的带碱量。
如图1所示，第四自蒸发器12的出料口、Ⅵ效蒸发器6的分离室出料口均通过母液出料泵16连接母液槽。
本实施例中，原液通过原液进料泵17分别向原液闪蒸器8、Ⅴ效蒸发器5输送原液。
本实施例中，Ⅰ～Ⅶ效蒸发器上盖顶部均设置了排不凝气系统18，以及时排出混入水蒸气的少量空气和其它不凝性气体。
各效蒸发器分离室的二次蒸汽出口与下一效蒸发器的加热室蒸汽进口连通，Ⅶ效蒸发器7的二次蒸汽出口与直接接触式水冷器19连通，利用直接接触水冷器19快速吸收二次蒸汽，使Ⅶ效蒸发器7的二次蒸汽加速逸出，提高蒸发效率；
新蒸汽管道与强制循环排盐蒸发器15的加热室蒸汽进口连通，强制循环排盐蒸发器15 的分离室二次蒸汽出口与Ⅵ效蒸发器6的加热室蒸汽进口连通，充分利用强制效循环排盐蒸发器15的分离室内产生的二次蒸汽。
第一级自蒸发器9二次蒸汽出口与Ⅱ效预热器14连通，第二级自蒸发器10～第四级自蒸发器12的二次蒸汽出口分别与Ⅳ效蒸发器4～Ⅵ效蒸发器6的加热室蒸汽进口连通。
原液闪蒸器8的二次蒸汽出口与Ⅵ效蒸发器6的加热室蒸汽进口连通，充分利用原液闪蒸器8的二次蒸汽；原液闪蒸器7内也设置有除沫器，以降低二次蒸汽的带碱量。
所述Ⅰ效蒸发器1上依次连接有Ⅰ效-1#冷凝水罐20-1～Ⅰ效-n#(n≤7)冷凝水罐20-n，Ⅰ效-n#冷凝水罐20-n连接一次冷凝水槽；Ⅰ效-1#冷凝水罐20-1～Ⅰ效-n#(n≤7)冷凝水罐20-n上分别设置有二次蒸汽出口，Ⅰ效-1#冷凝水罐20-1～Ⅰ效-n#(n≤7)冷凝水罐20-n 的二次蒸汽出口分别连接1～N(N≤Ⅶ)效蒸发器加热室蒸汽进口；Ⅰ效-n#冷凝水罐20-n的出水口与一次冷凝水泵21连通，Ⅰ效-n#冷凝水罐20-n内的一次冷凝水经一次冷凝水泵21 排入一次冷凝水槽。
本实施例中，n＝5，N＝Ⅴ，一次冷凝水经过5次闪蒸回收二次蒸汽进行再利用，充分回收一次冷凝水的热能，降低蒸发汽耗。
本实施例中的强制循环排盐蒸发器15的加热室下部与强制效冷凝水罐40连通，该强制效冷凝水罐40的二次蒸汽出口与强制循环排盐蒸发器15的加热室上部连通，强制效冷凝水罐40的出水口连接到Ⅰ效-5#冷凝水罐20-5的进水口，强制循环排盐蒸发器15的加热室内生成的一次冷凝水，通过强制效冷凝水罐40初次闪蒸后，进入Ⅰ效-5#冷凝水罐20-5再次闪蒸，生成的二次蒸汽进入Ⅴ效蒸发器5的加热室加热溶液。
所述Ⅱ效蒸发器2～Ⅶ效蒸发器7上分别对应连接有Ⅱ效冷凝水罐22～Ⅶ效冷凝水罐27，Ⅱ效冷凝水罐22～Ⅶ效冷凝水罐27依次串联，Ⅱ效冷凝水罐22～Ⅶ效冷凝水罐27上端均开设有蒸汽出口，Ⅱ效冷凝水罐22～Ⅶ效冷凝水罐27的蒸汽出口一一对应地连通到Ⅱ效蒸发器2～Ⅶ效蒸发器7的加热室蒸汽进口，Ⅶ效冷凝水罐27通过二次冷凝水泵28连接二次蒸汽冷凝水槽。
通过上述Ⅱ效冷凝水罐22～Ⅶ效冷凝水罐27的设置，对Ⅱ效蒸发器2～Ⅶ效蒸发器7生成的二次冷凝水的热能进行充分的回收利用，进一步降低蒸发汽耗。
Ⅰ效蒸发器1～Ⅴ效蒸发器5各自的分离室与加热室通过外部循环管路连通，循环管路上设置有循环泵29，循环泵29驱动本效蒸发器内的部分或全部溶液循环流动反复蒸发浓缩，上述各效蒸发器分离室的出料口通过过料泵30连接到上一效蒸发器的循环泵29进料口，从而将溶液直接送到上一效蒸发器的循环泵29进料口处，经上一效蒸发器的循环泵29送入上一效蒸发器的加热室内加热，避免溶液直接送入上一效蒸发器的分离室内而造成无效循环。比如Ⅲ效蒸发器3的分离室与加热室通过外部循环管路连通，循环管路上设置有循环泵29，Ⅲ效蒸发器3分离室内的部分溶液可通过循环泵29输送进Ⅲ效蒸发器3的加热室，形成循环回路，反复浓缩，Ⅲ效蒸发器3分离室内的部分也可通过过料泵30输送到Ⅱ效预热器14，经预热后自流进入Ⅱ效蒸发2的循环泵29进料口，经Ⅱ效蒸发器2的循环泵29输送到Ⅱ效蒸发器2的加热室进行加热，这样可确保从Ⅲ效蒸发器3分离室进入Ⅱ效蒸发器2的溶液全部进入Ⅱ效蒸发器2的加热室，而不会直接进入Ⅱ效蒸发器2的分离室，避免溶液的无效循环。
Ⅵ效蒸发器6、Ⅶ效蒸发器7各自的分离室与加热室同样通过外部的循环管路连通，循环管路上同样设置有循环泵29，Ⅶ效蒸发器7分离室的出料口通过过料泵30连接到Ⅵ效蒸发器6的循环泵29进料口；强制循环排盐蒸发器15的进料口通过强制循环进料泵31与第四自蒸发器12的出料口连通，强制循环排盐蒸发器15的分离室和加热室通过循环管路连通，循环管路上设置有强制循环泵32，强制循环排盐蒸发器15的出料口通过强制循环出料泵33 与盐沉降槽连通。
本实施例中Ⅰ效蒸发器1～Ⅶ效蒸发器7均为分体式结构，分别包括上下设置且相互连接的Ⅰ～Ⅶ效管式降膜加热室和Ⅰ～Ⅶ效集液室、并排设置在Ⅰ～Ⅶ效集液室一侧的Ⅰ～Ⅶ效分离室，Ⅰ～Ⅶ效集液室和Ⅰ～Ⅶ效分离室一一对应地通过各连通管连接。
由于Ⅰ效蒸发器1～Ⅶ效蒸发器7结构类似，为避免赘述，以Ⅰ效蒸发器1为例，详细说明Ⅰ效蒸发器1的分体式结构，Ⅱ～Ⅶ效蒸发器的分体式结构参照Ⅰ效蒸发器1。
如图2所示，Ⅰ效蒸发器1为分体式，包括上下设置且相互连接的Ⅰ效管式降膜加热室 1-1和Ⅰ效集液室1-2、并排设置在Ⅰ效集液室1-2一侧的Ⅰ效分离室1-3，Ⅰ效集液室1-2 和Ⅰ效分离室1-3通过连通管1-4连接。
Ⅰ效蒸发器1～Ⅶ效蒸发器7各自的集液室和分离室的底部均成锥形，第一～第四自蒸发器的底部也成锥形，溶液在其内流速较快，溶液易于冲刷，不易于产生沉积，避免结疤的产生，确保设备的传热效率。
分体式的Ⅰ效蒸发器1提供了更大的闪蒸空间，提高蒸发效率，Ⅰ效集液室1-2收集温度达到沸点的溶液后，将处于液面上的沸腾状态的溶液通过连通管1-4送入Ⅰ效分离室1-3 内闪蒸，确保进入Ⅰ效分离室1-3的溶液是处于沸腾状态的，确保闪蒸效果。
如图3所示，Ⅱ效蒸发器2的加热室蒸汽进口通过第一截止阀34与新蒸汽管道35连通，Ⅱ效蒸发器2的加热室蒸汽进口通过第二截止阀36与Ⅰ效蒸发器1的分离室二次蒸汽出口连通，Ⅱ效蒸发器2的分离室出料口通过第三截止阀37与第一自蒸发器9连通，Ⅱ效蒸发器2的分离室出料口通过第四截止阀38与Ⅰ效预热器13连通，所述Ⅰ效蒸发器1的分离室出料口通过第五截止阀39与第一自蒸发器9连通。
通过对第一～第五截止阀的控制，可将Ⅰ效蒸发器1单独隔离出来，并将新蒸汽进入Ⅱ效蒸发器2内，从而实现在Ⅰ效蒸发器1停机维护的时候，本实用新型所述七效管式降膜蒸发器组可当做六效管式降膜蒸发器组继续溶液的蒸发浓缩，从而降低生产成本，提高生产效率。
本实用新型的工作过程是：如图4～图6所示，采用上述七效管式降膜蒸发器对种分母液进行蒸发浓缩时，包括如下具体步骤：
a、引50％或55％或60％蒸发原液经依次串联的Ⅴ效蒸发器、Ⅳ效蒸发器、Ⅲ效蒸发器、Ⅱ效预热器、Ⅱ效蒸发器、Ⅰ效预热器、Ⅰ效蒸发器、第一自蒸发器、第二自蒸发器、第三自蒸发器、第四自蒸发器蒸发浓缩得到第一段出料母液，其中，Ⅰ效～Ⅴ效蒸发器各自的分离室与加热室通过循环管路连通，循环管路上设置有循环泵，各效蒸发器分离室内的溶液经过料泵输送到上一效蒸发器的循环泵进料口，其中Ⅲ效过料泵和Ⅱ效循环泵之间设有Ⅱ效预热器，Ⅱ效过料泵和Ⅰ效循环泵之间设有Ⅰ效预热器，比如Ⅲ效蒸发器的分离室与加热室通过外部的循环管路连通，循环管路上设置有循环泵，Ⅲ效蒸发器分离室内的部分溶液可通过循环泵输送进Ⅲ效蒸发器的加热室，形成循环回路，反复浓缩，Ⅲ效蒸发器分离室内的部分也可通过过料泵输送到Ⅱ效预热器，溶液经预热后自流入Ⅱ效蒸发器的循环泵进料口，经Ⅱ效蒸发器的循环泵输送到Ⅱ效蒸发器的加热室进行加热，这样可确保从Ⅲ效蒸发器分离室进入Ⅱ效蒸发器的溶液全部进入Ⅱ效蒸发器的加热室，而不会直接进入Ⅱ效蒸发器的分离室，避免溶液的无效循环。
b、经步骤a分流后的50％或45％或40％蒸发原液经依次串联的原液闪蒸器、Ⅶ效蒸发器、Ⅵ效蒸发器蒸发浓缩得到第二段出料母液；Ⅶ效蒸发器、Ⅵ效蒸发器各自的分离室与加热室通过外部的循环管路连通，循环管路上设置有循环泵，Ⅶ效蒸发器分离室内的溶液经过料泵输送到Ⅵ效蒸发器的循环泵进液口。
c、当溶液中的杂质(碳酸钠，硫酸钠等)含量超过工艺要求时，用强制循环进料泵引 20％～50％的第一段出料母液进强制循环排盐蒸发器进一步蒸发浓缩后排入盐沉降槽进行结晶排盐；强制循环排盐蒸发器的分离室和加热室通过循环管路连通，循环管路上设置有强制循环泵，完成蒸发浓缩的溶液由强制循环出料泵送入盐沉降槽。
d、将第一段出料母液与第二段出料母液经母液出料泵混合后输送至母液槽。
e、在进行步骤a～d的同时，引新蒸汽进入Ⅰ效蒸发器的加热室加热溶液，Ⅰ效蒸发器的分离室内产生的二次蒸汽进入Ⅱ效蒸发器的加热室加热溶液，Ⅱ效蒸发器的分离室内产生的二次蒸汽进入Ⅲ效蒸发器的加热室加热溶液，Ⅲ效蒸发器的分离室内产生的二次蒸汽进入Ⅳ效蒸发器的加热室加热溶液，Ⅳ效蒸发器的分离室内产生的二次蒸汽进入Ⅴ效蒸发器的加热室加热溶液，Ⅴ效蒸发器的分离室内产生的二次蒸汽进入Ⅵ效蒸发器的加热室加热溶液，Ⅵ效蒸发器的分离室内产生的二次蒸汽进入Ⅶ效蒸发器的加热室加热溶液，Ⅶ效蒸发器的分离室内产生的二次蒸汽进入直接接触式水冷器进行冷凝吸收；
f、进行步骤c时，引部分新蒸汽进入强制循环排盐蒸发器的加热室对其内溶液进行加热，由强制循环排盐蒸发器的分离室产生的二次蒸汽进入Ⅵ效蒸发器的加热室加热溶液；
g、进行步骤a和b时，由第一自蒸发器产生的二次蒸汽进入Ⅱ效预热器加热其内溶液、由第二自蒸发器、第三自蒸发器、第四自蒸发器产生的二次蒸汽分别进入Ⅳ效蒸发器的加热室、Ⅴ效蒸发器的加热室、Ⅵ效蒸发器的加热室加热溶液。
h、在进行步骤a～g的同时，Ⅰ效～Ⅶ效蒸发器的加热室产生的冷凝水由本效冷凝水罐收集，其中Ⅰ效蒸发器的加热室产生的一次冷凝水依次进入Ⅰ效-1#～Ⅰ效-n#(n≤7)冷凝水罐进行闪蒸，Ⅰ效-1#～Ⅰ效-n#(n≤7)冷凝水罐各自生成的二次蒸汽分别进入Ⅰ～N(N≤Ⅶ) 效蒸发器的加热室加热溶液，强制循环排盐蒸发器的加热室生成的一次冷凝水进入Ⅰ效-n# (n≤7)冷凝水罐闪蒸产生的二次蒸汽进入对应的N效蒸发器的加热室加热溶液；Ⅰ效-n# (n≤7)冷凝水罐内的一次冷凝水经一次冷凝水泵输送至一次冷凝水槽；Ⅱ～Ⅵ效蒸发器的加热室产生的二次冷凝水分别进入Ⅲ～Ⅶ效冷凝水罐进行多级闪蒸，Ⅱ～Ⅶ效冷凝水罐产生的二次蒸汽进入本效蒸发器的加热室加热溶液；二次冷凝水经二次冷凝水泵输送至二次冷凝水槽，其中n＝5、N＝Ⅴ。
步骤e中，在直接接触式水冷器的顶部设置真空泵接口并连接真空泵(如图1所示)，采用真空泵抽吸直接接触水冷器内的不凝性气体，使直接接触水冷器形成真空工况，加速二次蒸汽进入水冷器进行冷凝，确保Ⅶ效蒸发器分离室气压稳定，提高蒸发效率。
本实施例通过对原液分段浓缩、对各效蒸发器生成的二次蒸汽、各效冷凝水罐内闪蒸生成的二次蒸汽、强制循环排盐蒸发器15产生的二次蒸汽、第一～第四自蒸发器产生的二次蒸汽以及原液闪蒸器8产生的二次蒸汽进行充分的利用，大大提高了整个蒸发浓缩工艺的蒸发效率，使原液进料流量与传统七效蒸发工艺相比提高了约15％～25％，蒸水量提高了约15％～25％，而蒸发汽耗比则降低了20％左右，二次蒸汽冷凝水的带碱量也降低了约50％左右，大大提高了蒸发效率，降低了蒸发能耗，且降低了二次蒸汽带碱量。
以下是采用本实用新型所述种分母液七效蒸发浓缩工艺及七效管式降膜蒸发器组进行种分母液浓缩的蒸发效果与采用国内某厂家设计的种分母液七效蒸发浓缩工艺进行种分母液浓缩的的蒸发效果比对表(以400T/h七效管式降膜蒸发器组为例)：
上表中，循环冷却水即水冷器19所采用的用于冷却二次蒸汽的冷却水。
通过上表的对比可见，采用本实用新型所述种分母液七效蒸发浓缩工艺及七效管式降膜蒸发器组进行种分母液的浓缩，进料量、蒸水量、汽水比、二次蒸汽冷凝水含碱量、循环冷却水含碱量、循环冷却上下水含碱差值等各项指标均优于传统工艺的各项指标。
上述实施例仅例示性说明本发明创造的原理及其功效，以及部分运用的实施例，而非用于限制本发明；应当指出，对于本领域的普通技术人员来说，在不脱离本发明创造构思的前提下，还可以做出若干变形和改进，这些都属于本发明的保护范围。
Claims (6)
1.一种七效管式降膜蒸发器组，用于实施上述七效蒸发浓缩工艺，包括Ⅰ效蒸发器～Ⅶ效蒸发器，其特征在于，还包括原液闪蒸器、第一自蒸发器～第四自蒸发器、Ⅰ效预热器、Ⅱ效预热器以及强制循环排盐蒸发器，其中，Ⅴ效蒸发器、Ⅳ效蒸发器、Ⅲ效蒸发器、Ⅱ效预热器、Ⅱ效蒸发器、Ⅰ效预热器、Ⅰ效蒸发器、第一自蒸发器～第四自蒸发器依次联接形成第一段溶液浓缩回路；原液闪蒸器、Ⅶ效蒸发器、Ⅵ效蒸发器依次联接形成第二段溶液浓缩回路；经第一段溶液浓缩回路浓缩后的部分溶液分流进入强制循环排盐蒸发器形成第三段溶液浓缩回路；
各效蒸发器分离室的二次蒸汽出口与下一效蒸发器的加热室蒸汽进口连通，Ⅰ效蒸发器的蒸汽进口与新蒸汽管道连通，Ⅶ效蒸发器的二次蒸汽出口与水冷器连通；
强制循环排盐蒸发器加热室的蒸汽进口与新蒸汽管道连通，强制循环排盐蒸发器分离室的二次蒸汽出口与Ⅵ效蒸发器的加热室蒸汽进口连通；
第一级自蒸发器的二次蒸汽出口与Ⅱ效预热器连通，第二～第四级自蒸发器的二次蒸汽出口分别与Ⅳ～Ⅵ效蒸发器加热室蒸汽进口连通；
原液闪蒸器的二次蒸汽出口与Ⅶ效蒸发器加热室蒸汽进口连通；
所述Ⅰ效蒸发器上依次连接有Ⅰ效-1#～Ⅰ效-n#(n≤7)冷凝水罐，Ⅰ效-n#冷凝水罐通过一次冷凝水泵连接一次冷凝水槽；Ⅰ效-1#～Ⅰ效-n#(n≤7)冷凝水罐上分别设置有二次蒸汽出口，Ⅰ效-1#～Ⅰ效-n#(n≤7)冷凝水罐的二次蒸汽出口分别连接1～N(N≤Ⅶ)效蒸发器加热室蒸汽进口；
所述Ⅱ效蒸发器～Ⅶ效蒸发器上分别对应连接有Ⅱ效冷凝水罐～Ⅶ效冷凝水罐，Ⅱ效冷凝水罐～Ⅶ效冷凝水罐依次串联，Ⅱ效冷凝水罐～Ⅶ效冷凝水罐上端均开设有蒸汽出口，Ⅱ效冷凝水罐～Ⅶ效冷凝水罐的蒸汽出口一一对应地连通到Ⅱ效蒸发器～Ⅶ效蒸发器加热室的蒸汽进口，Ⅶ效冷凝水罐通过二次冷凝水泵连接二次冷凝水槽。
2.根据权利要求1所述的一种七效管式降膜蒸发器组，其特征在于，Ⅰ～Ⅶ效蒸发器上盖顶部均设置了排不凝气系统，以及时排出混入水蒸气的少量空气和不凝性气体。
3.根据权利要求1所述的一种七效管式降膜蒸发器组，其特征在于，Ⅰ～Ⅶ效蒸发器各自的分离室与加热室通过循环管路连通，循环管路上设置有循环泵，上述各效蒸发器分离室的出料口通过过料泵连接到上一效蒸发器的循环泵进料口，其中，Ⅲ效过料泵和Ⅱ效循环泵之间设有Ⅱ效预热器，Ⅱ效过料泵和Ⅰ效循环泵之间设有Ⅰ效预热器；Ⅵ效、Ⅶ效蒸发器各自的分离室与加热室通过循环管路连通，循环管路上设置有循环泵，Ⅶ效蒸发器分离室的出料口通过过料泵连接到Ⅵ效蒸发器的循环泵进料口；强制循环排盐蒸发器的进料口通过强制循环进料泵与第四自蒸发器的出料口连通，强制循环排盐蒸发器的分离室和加热室通过循环管路连通，循环管路上设置有强制循环泵，强制循环排盐蒸发器的出料口通过强制循环出料泵与盐沉降槽连通。
4.根据权利要求1所述的一种七效管式降膜蒸发器组，其特征在于，Ⅰ～Ⅶ效蒸发器均为分体式，分别包括上下设置且相互连接的Ⅰ～Ⅶ效管式降膜加热室和Ⅰ～Ⅶ效集液室、并排设置在Ⅰ～Ⅶ效集液室一侧的Ⅰ～Ⅶ效分离室，Ⅰ～Ⅶ效集液室和Ⅰ～Ⅶ效分离室一一对应地通过各连通管连接。
5.根据权利要求1所述的一种七效管式降膜蒸发器组，其特征在于，Ⅰ～Ⅶ效集液室、Ⅰ～Ⅶ效分离室的底部均成锥形，第一～第四自蒸发器的底部也成锥形。
6.根据权利要求1所述的一种七效管式降膜蒸发器组，其特征在于，Ⅱ效蒸发器的加热室蒸汽进口通过第一截止阀与新蒸汽管道连通，Ⅱ效蒸发器的加热室蒸汽进口通过第二截止阀与Ⅰ效蒸发器的分离室二次蒸汽出口连通，Ⅱ效蒸发器的分离室出料口通过第三截止阀与第一自蒸发器连通，Ⅱ效蒸发器的分离室出料口通过第四截止阀与Ⅰ效预热器连通，所述Ⅰ效蒸发器的分离室出料口通过第五截止阀与第一自蒸发器连通。
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