WO2016029614A1 - 脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置 - Google Patents

脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置 Download PDF

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WO2016029614A1
WO2016029614A1 PCT/CN2014/095969 CN2014095969W WO2016029614A1 WO 2016029614 A1 WO2016029614 A1 WO 2016029614A1 CN 2014095969 W CN2014095969 W CN 2014095969W WO 2016029614 A1 WO2016029614 A1 WO 2016029614A1
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sodium sulfate
filtrate
anhydrous sodium
purification treatment
temperature
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PCT/CN2014/095969
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French (fr)
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曹靖
吴光辉
王振云
范伟
张俊丰
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湖南江冶机电科技股份有限公司
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general

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  • the invention belongs to a resource recovery and utilization process, in particular to a method and a device for recovering anhydrous sodium sulfate from a filtrate after desulfurization lead paste purification treatment, and is used for recycling a lead from a waste lead-acid battery.
  • one of the important technical processes for the recovery of lead in waste lead-acid batteries by wet desulfurization-fire method is to add sodium carbonate to the lead-acid battery lead paste to convert lead sulfate into lead carbonate, and the desulfurization lead paste after the reaction.
  • the filtrate is purified and crystallized to prepare sodium sulfate, and then the lead carbonate is smelted to recover lead.
  • the crystallization of the filtrate to obtain anhydrous sodium sulfate is an important part of the process.
  • waste liquids containing sodium sulfate in industrial production. For example, chemical fiber, pesticide, white carbon black and other plants have sodium sulfate waste liquid to be treated to recover anhydrous sodium sulfate.
  • the source of the sodium sulphate-containing waste liquid is different, and the composition varies greatly.
  • the process for recovering anhydrous sodium sulphate from the waste liquid is also different. For example, for some low-concentration sodium sulphate waste liquid, evaporation and concentration crystallization must be used. Anhydrous sodium sulfate was recovered. Therefore, it is necessary to design a process technology that satisfies the recovery of anhydrous sodium sulfate from the filtrate after desulfurization of lead-acid paste purification treatment.
  • the method of recovering anhydrous sodium sulfate from the filtrate after desulfurization and lead paste purification treatment or from other waste liquids is basically a method of heating and evaporating crystallization.
  • the biggest disadvantage of this method is that the energy consumption is high, the product is easy to scale and crust in the evaporator, which greatly affects the evaporation efficiency and causes the blockage of the equipment pipeline.
  • energy consumption can be effectively reduced by using multi-effect evaporation or flashing technology, the problem of scale and crusting of equipment in actual production is always difficult to solve. If you can fix sodium sulfate decahydrate In the form of direct loss of crystal water and anhydrous sodium sulfate, the above problems can be avoided.
  • Sodium sulfate also known as Yuanming powder
  • Yuanming powder is an important chemical product.
  • the solubility of sodium sulfate in water below 40 °C is particularly sensitive to temperature changes. When it is lower than 37.2 °C, it is precipitated from the solution in the form of sodium sulfate decahydrate crystal.
  • the sodium sulfate decahydrate crystals can rapidly weather and lose the crystal water to become anhydrous sodium sulfate at a temperature higher than 40 ° C. Therefore, according to this characteristic and the concentration of sodium sulfate in the filtrate after desulfurization and lead paste purification treatment, the design is from desulfurization lead paste. After the purification treatment, the recovery of the anhydrous sodium sulfate from the filtrate is low, and the process technology of equipment maintenance is very necessary.
  • the existing evaporation method has problems such as high energy consumption, easy scaling of sodium sulfate in the equipment, and crusting.
  • a method for recovering anhydrous sodium sulfate from a filtrate after desulfurization and lead paste purification treatment comprises the following steps:
  • the temperature of the filtrate is lowered to -5 to 5 °C.
  • the drying temperature is maintained at 0 to 70 ° C, and the pressure is maintained at 0.01 to 100 mmHg until the crystals of sodium sulfate decahydrate loses 20% to 70%.
  • the drying temperature is maintained at 70 to 300 °C.
  • An apparatus for use in the above method comprising a filtrate storage tank, a freezing crystallization apparatus, a centrifuge, a low temperature vacuum dryer, and a drying apparatus which are sequentially connected by a pipe or a conveyor belt.
  • the filtrate storage tank has a pre-cooling facility; the low-temperature low-concentration sodium sulfate solution centrifugally separated after freezing and crystallization is sent to the filtrate storage tank pre-cooling facility through a self-priming pump through a self-priming pump as a cooling medium.
  • the low-temperature vacuum dryer is provided with a material weight display device, which can be used for real-time monitoring of weight loss during vacuum drying of materials.
  • the present invention recovers anhydrous sodium sulfate by a method of cryogenic freezing crystallization, and the obtained anhydrous sodium sulfate has higher purity and lower energy consumption.
  • the present invention can avoid the problem of scale and crusting of equipment caused by heating and evaporation.
  • Figure 1 is a block flow diagram of the apparatus of the present invention.
  • the 300 L filtrate of 28% by mass of sodium sulfate is sent to the freezing crystallization apparatus 2 to be cooled to -2 ° C, and the precipitated crystals are sent to the centrifuge for centrifugation, and the mother liquor is cooled at a low temperature.
  • the crystal product sodium sulfate decahydrate is sent to a low temperature vacuum dryer with a material weight display device, and vacuum dried to a weight of 40% at 55 ° C, the material is sent to the drying equipment at 110 ° C Under the conditions of normal pressure drying to constant weight, anhydrous sodium sulfate 65Kg.
  • the apparatus of the present invention comprises a filtrate storage tank with pre-cooling facilities, a freezing crystallization apparatus, a centrifuge, a low-temperature vacuum dryer with a material weight display device, and drying, which are sequentially connected by pipes or conveyor belts. device.
  • the filtrate having a concentration of sodium sulfate of 26% is sent to a freezing crystallization apparatus and cooled to 5 ° C.
  • the precipitated crystals are sent to the centrifuge for centrifugation, and the low temperature mother liquor is transported to the supernatant.
  • the crystalline product sodium sulfate decahydrate is sent to a low-temperature vacuum dryer with a material weight display device, and vacuum-dried at 50 ° C to 50% of the original weight.
  • the material was sent to a drying apparatus and dried under normal pressure to a constant weight at 110 ° C to obtain 50 Kg of anhydrous sodium sulfate.
  • the desulfurization lead paste in the filtrate storage tank is purified and treated with a concentration of 26% of sodium sulfate, and the filtrate is sent to a freezing crystallization apparatus and cooled to -5 ° C.
  • the precipitated crystals are sent to the centrifuge for centrifugation, and the low temperature mother liquor is transported.
  • the crystalline product sodium sulfate decahydrate is sent to a low-temperature vacuum dryer with a material weight display device, and vacuum-dried at 60 ° C to a weight of 60%.
  • the material was sent to a drying apparatus and dried at a constant pressure to a constant weight at 120 ° C to obtain 55 Kg of anhydrous sodium sulfate.
  • the method and device for recovering anhydrous sodium sulfate from the filtrate after purification treatment of the desulfurization lead paste of the invention realize direct conversion from sodium sulfate decahydrate to anhydrous sodium sulfate, and the energy consumption is low, and the sodium sulfate is easy to scale and knot in the equipment. ⁇ , easy to operate, easy to industrialize.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

提供一种脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置。该方法包括：冷冻结晶、低温真空干燥去除部分结晶水、烘干。该装置包括：通过管道或输送带依次连接的滤液储罐、冷冻结晶设备、离心机、低温真空干燥机和烘干设备。该方法从脱硫铅膏净化处理后的滤液中回收无水硫酸钠，避免环境污染，方法简单，易于实现工业化生产。

Description

脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置 技术领域
本发明属于资源回收和利用工艺，特别涉及一种脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置，用于从废铅酸蓄电池回收再生铅的工艺过程。
背景技术
目前湿法脱硫-火法冶炼回收废铅酸蓄电池中铅的重要技术工艺之一，是在废铅酸蓄电池铅膏中加入碳酸钠，使硫酸铅转变为碳酸铅，反应后的脱硫铅膏压滤滤液经净化、结晶制备硫酸钠的方法，然后碳酸铅火法冶炼回收铅。其中将滤液结晶得到无水硫酸钠是该工艺中的一个重要环节。此外工业生产中也有许多含硫酸钠的废液，如化纤、农药、白碳黑等厂均有硫酸钠废液需要处理回收无水硫酸钠。然而，含硫酸钠的废液来源不同，成份差异较大，从废液中回收无水硫酸钠的工艺方法也不同，比如，对于一些低浓度的硫酸钠废液必须采用蒸发浓缩结晶的方法来回收无水硫酸钠。因此，有必要设计一种符合从脱硫铅膏净化处理后滤液回收无水硫酸钠的工艺技术。
目前，不论是从脱硫铅膏净化处理后滤液还是从其它废液中回收无水硫酸钠的方法基本上都是采用加热蒸发结晶的方法。但这种方法最大的缺点是能耗高、产品极易在蒸发器中结垢、结疤，大大影响蒸发效率和造成设备管道堵塞的现象。虽然通过采用多效蒸发或闪蒸技术能有效降低能耗，但实际生产中设备结垢、结疤问题始终难以解决。如能将十水硫酸钠以固 态形式的直接失去结晶水变无水硫酸钠，则可避免上述问题。然而，想要直接加热十水硫酸钠去结晶水存在很大困难，因为加热过程中十水硫酸钠会吸潮、融化变液态。
硫酸钠，又名元明粉，是一种重要的化工产品，硫酸钠水溶液40℃以下在水中溶解度对温度变化特别敏感，在低于37.2℃时以十水硫酸钠晶体形式从溶液中析出。而十水硫酸钠晶体在高于40℃时能迅速风化失去结晶水成为无水硫酸钠，因此根据这一特性以及脱硫铅膏净化处理后滤液硫酸钠浓度较大实际情况，设计从脱硫铅膏净化处理后滤液回收无水硫酸钠的能耗较低，设备维护简单的工艺技术是非常必要的。
技术问题
现有的蒸发方法，存在能耗高、硫酸钠在设备中易结垢、结疤等问题。
技术解决方案
本发明解决上述技术问题的技术方案为：
一种脱硫铅膏净化处理后滤液回收无水硫酸钠的方法，包括如下步骤：
(1)冷冻结晶：将滤液降低温度，缓慢搅拌下析出十水硫酸钠晶体，进入离心机分离；
(2)真空干燥：将步骤(1)所得十水硫酸钠晶体，置于低温真空干燥机抽真空干燥至晶体表面不再有晶体光泽，此时部分结晶水脱去；
(3)烘干：将步骤(2)所得十水硫酸钠晶体部分脱水产物，置于烘干机上进一步干燥脱水得无水硫酸钠产品。
所述步骤(1)中，滤液温度降低至-5～5℃。
所述步骤(2)中，干燥温度维持在0～70℃，压力保持在0.01～100mmHg，直到十水硫酸钠晶体失重20％～70％。
所述步骤(3)中，干燥温度维持在70～300℃。
一种用于上述的方法的装置，包括通过管道或输送带依次连接的滤液储罐、冷冻结晶设备、离心机、低温真空干燥机和烘干设备。
所述的滤液储罐带有预冷设施；冷冻结晶后离心分离出的温度较低的低浓度硫酸钠溶液通过自吸泵经保温管道输送至滤液储罐预冷设施中作为冷却介质。
所述的低温真空干燥机带有物料重量显示装置，可用于实时监控物料真空干燥时的失重情况。
有益效果
本发明的有益效果在于：
(1)本发明采用低温冷冻结晶的方法回收无水硫酸钠，所得无水硫酸钠纯度更高、所需能耗更低。
(2)本发明能够避免加热蒸发带来的设备结垢、结疤问题。
附图说明
图1是本发明的设备流程框图。
本发明的最佳实施方式
滤液储罐中的脱硫铅膏净化处理后硫酸钠质量百分比浓度28％的300L滤液，送入冷冻结晶设备2中冷却到-2℃，析出结晶连同母液送入离心机中离心分离，低温的母液输送至滤液储罐的预冷设施中作为冷却介质，结 晶产物十水硫酸钠送入带有物料重量显示装置的低温真空干燥机，在55℃的条件下真空干燥至重量为原来的40％时，将此物料送入烘干设备中，在110℃的条件下常压干燥至恒重，得无水硫酸钠65Kg。
本发明的实施方式
如图1所示，本发明的装置包括通过管道或输送带依次连接的带有预冷设施的滤液储罐、冷冻结晶设备、离心机、带有物料重量显示装置的低温真空干燥机和烘干设备。
实施例1
滤液储罐中的脱硫铅膏净化处理后硫酸钠质量百分比浓度26％的250L滤液，送入冷冻结晶设备中冷却到5℃，析出结晶连同母液送入离心机中离心分离，低温的母液输送至滤液储罐的预冷设施中作为冷却介质，结晶产物十水硫酸钠送入带有物料重量显示装置的低温真空干燥机，在50℃的条件下真空干燥至重量为原来的50％时，将此物料送入烘干设备中，在110℃的条件下常压干燥至恒重，得50Kg无水硫酸钠。
实施例2
滤液储罐中的脱硫铅膏净化处理后硫酸钠质量百分比浓度26％的250L滤液，送入冷冻结晶设备中冷却到-5℃，析出结晶连同母液送入离心机中离心分离，低温的母液输送至滤液储罐的预冷设施中作为冷却介质，结晶产物十水硫酸钠送入带有物料重量显示装置的低温真空干燥机，在60℃的条件下真空干燥至重量为原来的60％时，将此物料送入烘干设备中，在120℃的条件下常压干燥至恒重，得无水硫酸钠55Kg。
工业实用性
本发明的脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置，实现直接由十水硫酸钠固态转变成无水硫酸钠，能耗低，硫酸钠在设备中易结垢、结疤，操作简单，易于工业化推广。

Claims (7)

  1. 一种脱硫铅膏净化处理后滤液回收无水硫酸钠的方法，包括如下步骤：
    (1)冷冻结晶：将滤液降低温度，搅拌析出十水硫酸钠晶体，进入离心机分离；
    (2)真空干燥：将步骤(1)所得十水硫酸钠晶体，置于低温真空干燥机抽真空干燥至晶体表面无晶体光泽，即部分结晶水；
    (3)烘干：将步骤(2)所得十水硫酸钠晶体部分脱水产物，置于烘干机上进一步干燥脱水得无水硫酸钠产品。
  2. 根据权利要求1所述的脱硫铅膏净化处理后滤液回收无水硫酸钠的方法，所述步骤(1)中滤液温度降低至-5～5℃。
  3. 根据权利要求1所述的脱硫铅膏净化处理后滤液回收无水硫酸钠的方法，所述步骤(2)中，干燥温度维持在0～70℃，压力保持在0.01～100mmHg，直到十水硫酸钠晶体失重20％～70％。
  4. 根据权利要求1所述的脱硫铅膏净化处理后滤液回收无水硫酸钠的方法，所述步骤(3)中干燥温度维持在70～300℃。
  5. 一种用于权利要求1至4任一项所述的方法的装置，包括通过管道或输送带依次连接的滤液储罐、冷冻结晶设备、离心机、低温真空干燥机和烘干设备。
  6. 根据权利要求5所述的装置，所述的滤液储罐带有预冷设施；冷冻结晶后离心分离出的温度较低的低浓度硫酸钠溶液通过自吸泵经保温管道输送至滤液储罐预冷设施中作为冷却介质。
  7. 根据权利要求5所述的装置，所述的低温真空干燥机带有物料重量显 示装置，用于实时监控物料真空干燥时的失重情况。
PCT/CN2014/095969 2014-08-25 2014-12-31 脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置 WO2016029614A1 (zh)

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101602514A (zh) * 2008-06-10 2009-12-16 四川川眉特种芒硝有限公司 一种高纯度特种芒硝的制造方法
CN102452674A (zh) * 2010-11-01 2012-05-16 中国石油化工股份有限公司 一种从乙烯装置废碱液中回收硫酸钠的处理方法
CN103771459A (zh) * 2014-01-16 2014-05-07 北京化工大学 一种从含铅脱硫废液中回收硫酸钠的方法
CN104140115A (zh) * 2014-08-25 2014-11-12 湖南江冶机电科技股份有限公司 脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100375714C (zh) * 2006-04-14 2008-03-19 中盐制盐工程技术研究院 一种冷冻法无水硝生产工艺
CN101844781B (zh) * 2010-05-20 2012-07-25 四川省川眉芒硝有限责任公司 一种高纯度无水芒硝的制造工艺
CN102515207A (zh) * 2011-12-13 2012-06-27 宜宾天原集团股份有限公司 一种从脱氯淡盐水中回收硫酸根制取无水芒硝的方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101602514A (zh) * 2008-06-10 2009-12-16 四川川眉特种芒硝有限公司 一种高纯度特种芒硝的制造方法
CN102452674A (zh) * 2010-11-01 2012-05-16 中国石油化工股份有限公司 一种从乙烯装置废碱液中回收硫酸钠的处理方法
CN103771459A (zh) * 2014-01-16 2014-05-07 北京化工大学 一种从含铅脱硫废液中回收硫酸钠的方法
CN104140115A (zh) * 2014-08-25 2014-11-12 湖南江冶机电科技股份有限公司 脱硫铅膏净化处理后滤液回收无水硫酸钠的方法及其装置

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106946395A (zh) * 2017-05-09 2017-07-14 北京天地人环保科技有限公司 一种脱硫废水分质结晶处理的方法及装置
CN110937611A (zh) * 2019-11-01 2020-03-31 临涣焦化股份有限公司 一种提高脱硫废液副盐纯度的系统及方法
CN110937611B (zh) * 2019-11-01 2023-05-23 临涣焦化股份有限公司 一种提高脱硫废液副盐纯度的系统及方法
CN111410354A (zh) * 2020-04-29 2020-07-14 河南碧云环保工程有限公司 一种脱硫脱硝废液的循环回收再利用系统及其处理脱硫脱硝废液的方法
CN112707416A (zh) * 2020-12-30 2021-04-27 广西天源新能源材料有限公司 一种基于锂聚合物的元明粉制备方法

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