CN106082516A - 一种分盐结晶工艺和装置 - Google Patents
一种分盐结晶工艺和装置 Download PDFInfo
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- CN106082516A CN106082516A CN201610547062.3A CN201610547062A CN106082516A CN 106082516 A CN106082516 A CN 106082516A CN 201610547062 A CN201610547062 A CN 201610547062A CN 106082516 A CN106082516 A CN 106082516A
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- salt
- nanofiltration
- rization system
- water
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- 238000000034 method Methods 0.000 title claims abstract description 41
- 239000006002 Pepper Substances 0.000 title claims abstract description 33
- 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 75
- 238000001728 nano-filtration Methods 0.000 claims abstract description 71
- 239000011780 sodium chloride Substances 0.000 claims abstract description 57
- 239000000243 solution Substances 0.000 claims abstract description 39
- FAPWRFPIFSIZLT-UHFFFAOYSA-M sodium chloride Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 35
- 239000012466 permeate Substances 0.000 claims abstract description 34
- 150000003839 salts Chemical class 0.000 claims abstract description 32
- 239000012528 membrane Substances 0.000 claims abstract description 29
- 239000012267 brine Substances 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 18
- 238000002425 crystallisation Methods 0.000 claims abstract description 15
- 230000005712 crystallization Effects 0.000 claims abstract description 15
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound 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[Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 14
- 239000010446 mirabilite Substances 0.000 claims abstract description 13
- 230000000694 effects Effects 0.000 claims description 35
- FGIUAXJPYTZDNR-UHFFFAOYSA-N Potassium nitrate Chemical compound 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[Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- KEAYESYHFKHZAL-UHFFFAOYSA-N sodium Chemical compound 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[Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-N Carbonic acid Chemical compound 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- 239000006228 supernatant Substances 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water, or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
- C02F5/06—Softening water by precipitation of the hardness using calcium compounds
Abstract
本发明提供了一种分盐结晶工艺，包括：使盐水经过纳滤膜以得到纳滤透过液和纳滤浓缩液；使纳滤浓缩液和纳滤透过液通过膜浓缩设备以得到产水和浓水；使浓水进入蒸发系统进行浓缩结晶；以及对结晶进行脱水干燥，得到精纯盐或者无水硝。该工艺可实现从污水处理站难处理的浓盐水中提取出高纯度的盐和无水硝，实现废水资源化，具有流程短、设备集中、占地小、能耗低的特点。
Description
技术领域
[0001]本发明涉及环保技术领域，具体涉及一种浓盐水通过膜分离浓缩和两效蒸发结晶实现零排放及分盐结晶的工艺和相关的装置。
背景技术
[0002]我国山西、内蒙等地均是水资源缺乏地区，有许多企业受缺水的困扰，常常出现企业与农业或其他工业争水现象。因此，在污水达标处理的基础上，开展污水的深度处理，最大限度地实现省水、节水和回用具有重大意义。另一方面，随着新的水十条、新环保法以及即将颁布的含盐废水控制排放标准，浓盐水零排放势在必行。“零排放”是不向地表水域排放任何形式的废水，将项目产生的浓盐水浓缩成为固体或浓缩液的形式再加以处理。
[0003]现有零排放技术是采取蒸发结晶对浓盐水进行处置，消耗大量的蒸汽能源、占地大，同时产生大量混盐。混盐或被作为危险废物处理，或送去填埋，造成资源浪费。因此，有必要寻找一种环保、绿色无污染且可以实现资源的回收利用的新技术。
发明内容
[0004]本发明的目的在于克服上述现有技术的缺陷，提供一种浓盐水通过膜分离浓缩和两效蒸发结晶实现零排放及分盐结晶的工艺。
[0005]根据本发明的一个方面，提供了一种分盐结晶工艺，包括:使盐水经过纳滤膜以得到纳滤透过液和纳滤浓缩液;使所述纳滤浓缩液和所述纳滤透过液通过膜浓缩设备以得到产水和浓水;使所述浓水进入蒸发系统进行浓缩结晶；以及对所述结晶进行脱水干燥，得到精纯盐或者无水硝。
[0006] 在上述分盐结晶工艺，在所述使盐水经过纳滤膜以得到纳滤透过液和纳滤浓缩液的步骤之前，还包括:通过化学沉淀法去除所述盐水中的金属离子，其中，所述盐水为总溶解性固体在45000〜55000mg/L范围内的浓盐水。
[0007] 在上述分盐结晶工艺，所述使盐水经过纳滤膜以得到纳滤透过液和纳滤浓缩液的步骤进一步包括:使所述盐水经一级纳滤膜分离浓缩，得到一级纳滤透过液和一级纳滤浓缩液;使所述一级纳滤透过液通过二级纳滤膜分离浓缩得到二级纳滤透过液和二级纳滤浓缩液。
[0008] 在上述分盐结晶工艺，所述使所述纳滤浓缩液和所述纳滤透过液通过膜浓缩设备以得到产水和浓水的步骤进一步包括:使所述一级纳滤浓缩液和所述二级纳滤浓缩液通过中间水箱混合后，进入膜浓缩设备I，进一步浓缩分离得到产水I和浓水I;使所述二级纳滤透过液进入膜浓缩设备2，得到产水2和浓水2。
[0009]在上述分盐结晶工艺，对所述结晶进行脱水干燥得到精纯盐或者无水硝的步骤进一步包括:使所述浓水I经钛板换热器预热升温后进入第一效蒸发系统进行浓缩结晶，得到硝浆;移出第一效蒸发系统的析硝母液，闪蒸;使降温后的析硝母液和浓水2经中间水箱混合后，进入第二效蒸发系统浓缩结晶得到盐浆。
[0010]在上述分盐结晶工艺，对所述结晶进行脱水干燥，得到精纯盐或者无水硝的步骤进一步包括:对所述硝浆进行脱水、干燥，得到产品无水硝;所述对盐浆进行脱水、干燥，得到广品精纯盐。
[0011] 在上述分盐结晶工艺，通过石灰纯碱法对所述盐水进行化学沉淀。
[0012]在上述分盐结晶工艺，所述一级纳滤浓缩液的总溶解性固体为70000〜75000mg/L，所述一级纳滤透过液的总溶解性固体为47000〜48000mg/L;所述二级纳滤浓缩液的总溶解性固体为61000〜63000mg/L，所述二级纳滤透过液的总溶解性固体为45000〜47000mg/L ；所述产水I的总溶解性固体为3200〜3600mg/L，所述浓水I的总溶解性固体为110000〜120000mg/L，所述浓水I含80-85%的NaCl以及15〜18%的Na2SO4;所述产水2的总溶解性固体为2300〜2500mg/L，所述浓水2的总溶解性固体为90000〜110000mg/L，所述浓水2含97〜99%的NaCl;所述第一效蒸发系统的蒸发浓缩温度为95〜105°C;所述第二效蒸发系统的蒸发浓缩温度为35〜50 °C。
[0013]根据本发明的另一方面，还提供了一种分盐结晶装置，其特征在于，包括:依次连接的加药系统、浓盐水反应槽、沉淀池、一级纳滤膜设备、膜浓缩设备1、第一效蒸发系统、闪蒸罐、中间水箱以及第二效蒸发系统；以及连接在所述一级纳滤膜设备和所述中间水箱之间的二级纳滤膜设备以及膜浓缩设备2。
[0014]在上述分盐结晶装置中，所述第一效蒸发系统与所述膜浓缩设备I的浓缩液出口连接，以对浓缩液进行蒸发浓缩结晶处理;所述第二效蒸发系统与所述中间水箱的出口连接，以对混合液进行蒸发浓缩结晶处理;所述闪蒸罐与所述第一效蒸发系统的析硝母液连接，以对从所述第一效蒸发系统移出的析硝母液进行闪蒸降温;所述第一效蒸发系统的硝浆出口依次连接第一离心机、第一流化床干燥包装机;所述第二效蒸发系统的盐浆出口依次连接第二离心机、第二流化床干燥包装机。
[0015]与现有技术相比，本发明的有益效果是:
[0016] I)通过对浓盐水的一系列处理可实现零排放及分盐结晶，生产出高质量的盐和无水硝;从废水提取出有价值的产品。
[0017] 2迪水先去除钙镁离子，再经纳滤分离、膜浓缩，得到浓水I中Na2SO4的浓度接近饱和状态，浓水2中NaCl的浓度接近饱和状态。进入蒸发结晶系统的浓水量大幅度减少，只占原水量的25-60%，降低了蒸发系统的设备、占地成本及运行费用，同时提高了提硝效率；
[0018] 3)膜浓缩设备透过液即产水的杂质浓度极低，可用于工厂生产用水；
[0019] 4)采用膜分离浓缩加两效蒸发结晶实现零排放及分盐结晶具有流程短、设备少、占地小的特点，可节省投资和运行成本。另外该发明能耗低，比传统的多效真空制盐节省了大量能源，同时减少了对锅炉设备的依赖，无污染物，更环保，适合于缺水地区推广。
[0020] 该工艺可实现从污水处理站难处理的浓盐水中提取出高纯度的盐和无水硝，实现废水资源化，具有流程短、设备集中、占地小、能耗低的特点。本发明可使浓盐水资源化，实现零排放及分盐结晶，解决上述难题，并产出有经济价值的产品。
附图说明
[0021]图1是本发明的实施例的一种浓盐水零排放及分盐结晶工艺的流程示意图。
[0022]图2是本发明的实施例的一种浓盐水零排放及分盐结晶装置的结构示意图。
具体实施方式
[0023]下面结合附图和具体实施例对本发明作进一步详细说明。
[0024] 实施例1
[0025] —种浓盐水零排放及分盐结晶的工艺包括以下步骤:
[0026] I)取浓盐水，其NaCl浓度为24〜28g/L，往浓盐水中投加石灰和纯碱使钙镁等高价金属离子发生化学反应生成钙、镁等的盐类沉淀物；
[0027] 2)产生沉淀后，上清液进入一级纳滤膜设备，得到一级纳滤透过液和一级纳滤浓缩液。
[0028] 3) —级纳滤透过液进入二级纳滤膜设备，得到二级纳滤透过液和二级纳滤浓缩液。由于纳滤膜对硫酸根的截留率达到95%以上，经纳滤膜分离后，其透过液中硫酸根的含量极低，SO42^ 2.5g/L，而浓缩液中硫酸钠的浓度进一步提高。
[0029] 4)—级纳滤浓缩液和二级纳滤浓缩液在中间水箱混合后进入膜浓缩设备I，得到膜浓缩设备透过液即产水I和膜浓缩设备浓缩液即浓水I。经过膜浓缩设备I，截留了较多Na2SO4的纳滤膜浓缩液得到进一步浓缩，得到浓水I，其中Na2SO4浓度在15〜18 %之间，接近饱和状态。
[0030] 5)浓水I经钛板换热器预热升温后进入第一效蒸发结晶系统，蒸发温度控制在95〜105°C之间，这时Na2SO4在该温度下处于过饱和状态，不断析出无水硫酸钠晶体，得到硝浆，硝浆进行离心脱水分离得湿硝，湿硝进入流化床干燥后包装得硝产品。
[0031] 6)步骤5)中无水硫酸钠晶体析出后，析硝母液中因闪蒸而NaCl不断的被浓缩，使得析硝母液的NaCl含量较高。经先闪蒸后降温的析硝母液进一步得到浓缩，NaCl浓度接近饱和状态。
[0032] 7) 二级纳滤透过液进入膜浓缩设备2得到进一步浓缩，膜浓缩设备2透过液即产水
2可作为工业生产水。膜浓缩设备2浓缩液即浓水2中NaCl浓度接近饱和状态。
[0033] 8)浓缩降温后的析硝母液与浓水2混合后进入第二效蒸发结晶系统，蒸发温度控制在35〜50°C之间，这时盐不断析出，得到盐浆，盐浆进行离心脱水分离得湿盐，湿盐进入流化床干燥后包装得盐产品。
[0034] 其中，步骤I)中浓盐水的TDS(总溶解性固体)为45000〜55000mg/L;并且在步骤I)中，通过石灰纯碱法对浓盐水进行化学沉淀；
[0035] 其中，步骤2)中一级纳滤浓缩液的TDS为70000〜75000mg/L，一级纳滤透过液的TDS为47000〜48000mg/L；
[0036] 其中，步骤3)中二级纳滤浓缩液的TDS为61000〜63000mg/L，二级纳滤透过液的TDS为45000〜47000mg/L；
[0037] 其中，步骤4)中产水I的TDS为3200〜3600mg/L，浓水I的TDS为110000〜120000mg/L，含NaC180-85%，Na2S0415〜18%。
[0038] 其中，步骤5)中产水2的TDS为2300〜2500mg/L，浓水2的TDS为90000〜I1000mg/L，含 NaC197 〜99%。
[0039]其中，步骤6)中的蒸发浓缩温度为95〜105°C ；
[0040]其中，步骤8)中的蒸发浓缩温度为35〜50°C。
[0041] 该工艺可实现从污水处理站难处理的浓盐水中提取出高纯度的盐和无水硝，实现废水资源化，具有流程短、设备集中、占地小、能耗低的特点。
[0042] 实施例2
[0043] 一种浓盐水零排放及分盐结晶装置，其包括顺次连接的加药系统(1)、浓盐水反应槽(2)、沉淀池(3)、一级纳滤膜设备(4)、膜浓缩设备I (5)、钛板换热器(6)、第一效蒸发系统
(7)、闪蒸罐(8)、中间水箱(9)、第二效蒸发系统(10)以及连接在一级纳滤膜设备(4)和中间水箱(9)之间的二级纳滤膜设备(15)以及膜浓缩设备2(16)。第一效蒸发系统(7)与膜浓缩设备1(5)的浓缩液出口连接，以对浓缩液进行蒸发浓缩结晶处理;第二效蒸发系统(10)与中间水箱(9)(混合了浓缩并降温后的析硝母液和16膜浓缩设备2出口浓缩液)的出口连接，以对混合液进行蒸发浓缩结晶处理；闪蒸罐(8)与第一效蒸发系统(7)的析硝母液连接，以对从第一效蒸发系统(7)移出的析硝母液进行闪蒸降温;第一效蒸发系统(7)的硝浆出口依次连接第一离心机(13)、第一流化床干燥包装机(14);第二效蒸发系统(10)的盐浆出口依次连接第二离心机(11)、第二流化床干燥包装机(12)。
[0044]该装置采用膜分离浓缩加两效蒸发结晶实现零排放及分盐结晶具有流程短、设备少、占地小的特点，可节省投资和运行成本。另外该装置所需能耗低，比传统的多效真空制盐节省了大量能源，同时减少了对锅炉设备的依赖，无污染物，更环保，适合于缺水地区推广。
[0045]上述实施例仅为本发明的优选实施方式，不能以此来限定本发明的保护范围，本领域的技术人员在本发明的基础上所做的任何非实质性的变化及替换均属于本发明的保护范围。
Claims (10)
1.一种分盐结晶工艺，其特征在于，包括: 使盐水经过纳滤膜以得到纳滤透过液和纳滤浓缩液； 使所述纳滤浓缩液和所述纳滤透过液通过膜浓缩设备以得到产水和浓水； 使所述浓水进入蒸发系统进行浓缩结晶；以及 对所述结晶进行脱水干燥，得到精纯盐或者无水硝。
2.根据权利要求1所述的分盐结晶工艺，其特征在于，在所述使盐水经过纳滤膜以得到纳滤透过液和纳滤浓缩液的步骤之前，还包括: 通过化学沉淀法去除所述盐水中的金属离子，其中，所述盐水为总溶解性固体在45000〜55000mg/L范围内的浓盐水。
3.根据权利要求1所述的分盐结晶工艺，其特征在于，所述使盐水经过纳滤膜以得到纳滤透过液和纳滤浓缩液的步骤进一步包括: 使所述盐水经一级纳滤膜分离浓缩，得到一级纳滤透过液和一级纳滤浓缩液； 使所述一级纳滤透过液通过二级纳滤膜分离浓缩得到二级纳滤透过液和二级纳滤浓缩液。
4.根据权利要求3所述的分盐结晶工艺，其特征在于，所述使所述纳滤浓缩液和所述纳滤透过液通过膜浓缩设备以得到产水和浓水的步骤进一步包括: 使所述一级纳滤浓缩液和所述二级纳滤浓缩液通过中间水箱混合后，进入膜浓缩设备I，进一步浓缩分离得到产水I和浓水I; 使所述二级纳滤透过液进入膜浓缩设备2，得到产水2和浓水2。
5.根据权利要求4所述的分盐结晶工艺，其特征在于，对所述结晶进行脱水干燥得到精纯盐或者无水硝的步骤进一步包括: 使所述浓水I经钛板换热器预热升温后进入第一效蒸发系统进行浓缩结晶，得到硝浆； 移出第一效蒸发系统的析硝母液，闪蒸； 使降温后的析硝母液和浓水2经中间水箱混合后，进入第二效蒸发系统浓缩结晶得到盐浆。
6.根据权利要求5所述的分盐结晶工艺，其特征在于，对所述结晶进行脱水干燥，得到精纯盐或者无水硝的步骤进一步包括: 对所述硝浆进行脱水、干燥，得到产品无水硝； 所述对盐浆进行脱水、干燥，得到产品精纯盐。
7.根据权利要求2所述的分盐结晶工艺，其特征在于，通过石灰纯碱法对所述盐水进行化学沉淀。
8.根据权利要求5所述的分盐结晶工艺，其中: 所述一级纳滤浓缩液的总溶解性固体为70000〜75000mg/L，所述一级纳滤透过液的总溶解性固体为47000〜48000mg/L; 所述二级纳滤浓缩液的总溶解性固体为61000〜63000mg/L，所述二级纳滤透过液的总溶解性固体为45000〜47000mg/L; 所述产水I的总溶解性固体为3200〜3600mg/L，所述浓水I的总溶解性固体为110000〜120000mg/L，所述浓水 I 含80-85 % 的 NaCl 以及15〜18 % 的 Na2SO4 ； 所述产水2的总溶解性固体为2300〜2500mg/L，所述浓水2的总溶解性固体为90000〜110000mg/L，所述浓水2含97〜99% 的NaCl ； 所述第一效蒸发系统的蒸发浓缩温度为95〜105°C ; 所述第二效蒸发系统的蒸发浓缩温度为35〜50°C。
9.一种分盐结晶装置，其特征在于，包括: 依次连接的加药系统、浓盐水反应槽、沉淀池、一级纳滤膜设备、膜浓缩设备1、第一效蒸发系统、闪蒸罐、中间水箱以及第二效蒸发系统；以及 连接在所述一级纳滤膜设备和所述中间水箱之间的二级纳滤膜设备以及膜浓缩设备2。
10.根据权利要求9所述的分盐结晶装置，其特征在于， 所述第一效蒸发系统与所述膜浓缩设备I的浓缩液出口连接，以对浓缩液进行蒸发浓缩结晶处理； 所述第二效蒸发系统与所述中间水箱的出口连接，以对混合液进行蒸发浓缩结晶处理； 所述闪蒸罐与所述第一效蒸发系统的析硝母液连接，以对从所述第一效蒸发系统移出的析硝母液进行闪蒸降温； 所述第一效蒸发系统的硝浆出口依次连接第一离心机、第一流化床干燥包装机； 所述第二效蒸发系统的盐浆出口依次连接第二离心机、第二流化床干燥包装机。
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