CN103011461A - Method of removing antimony (III) in source water by combining ferric salt coagulation pretreatment and ultrafiltration short flow process - Google Patents
Method of removing antimony (III) in source water by combining ferric salt coagulation pretreatment and ultrafiltration short flow process Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 148
- 238000000034 method Methods 0.000 title claims abstract description 74
- 238000000108 ultra-filtration Methods 0.000 title claims abstract description 63
- 150000003839 salts Chemical class 0.000 title claims abstract description 40
- 238000005345 coagulation Methods 0.000 title claims abstract description 26
- 230000015271 coagulation Effects 0.000 title claims abstract description 26
- TXTQARDVRPFFHL-UHFFFAOYSA-N [Sb].[H][H] Chemical compound [Sb].[H][H] TXTQARDVRPFFHL-UHFFFAOYSA-N 0.000 title 1
- FAWGZAFXDJGWBB-UHFFFAOYSA-N antimony(3+) Chemical compound [Sb+3] FAWGZAFXDJGWBB-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000012528 membrane Substances 0.000 claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 6
- 238000005189 flocculation Methods 0.000 claims abstract description 6
- 230000016615 flocculation Effects 0.000 claims abstract description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
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- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 claims description 2
- 239000003814 drug Substances 0.000 claims 1
- 239000003651 drinking water Substances 0.000 abstract description 19
- 235000020188 drinking water Nutrition 0.000 abstract description 19
- 230000000694 effects Effects 0.000 abstract description 5
- 238000000746 purification Methods 0.000 abstract description 4
- 150000002505 iron Chemical class 0.000 abstract description 3
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 abstract description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 abstract description 2
- 238000002203 pretreatment Methods 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000013618 particulate matter Substances 0.000 description 4
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 3
- 238000000975 co-precipitation Methods 0.000 description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000013043 chemical agent Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
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- 239000002384 drinking water standard Substances 0.000 description 2
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- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 description 1
- ZDINGUUTWDGGFF-UHFFFAOYSA-N antimony(5+) Chemical compound [Sb+5] ZDINGUUTWDGGFF-UHFFFAOYSA-N 0.000 description 1
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Abstract
一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，它涉及一种饮用水突发性污染净化处理方法，具体涉及一种三价铁盐混凝预处理联合超滤短流程工艺去除水中三价锑的方法，本发明是要解决现有饮用水处理方法不适用于突发性的水源水三价锑污染，尤其当水源水中三价锑浓度达30~150μg/L时应用现有饮用水处理方法对污染水体进行净化处理后不能达到《生活饮用水卫生标准》对水中三价锑的浓度要求的技术问题，方法如下：向水体中加入三价铁盐，先入絮凝反应池再经超滤池过滤。净化方法节省成本，操作方便，处理后可使出厂水中三价锑的浓度降低至1~3μg/L，效果显著，可作为超滤膜水厂或农村小型水厂应急处理方案。
A method for removing trivalent antimony in water source water by combining trivalent iron salt coagulation pretreatment with ultrafiltration short-flow process, which relates to a purification treatment method for sudden pollution of drinking water, in particular to a ferric salt coagulation pretreatment method A method for removing trivalent antimony in water combined with an ultrafiltration short process process, the present invention is to solve the problem that the existing drinking water treatment method is not suitable for sudden trivalent antimony pollution in water source water, especially when the concentration of trivalent antimony in water source water reaches 30 When ~150μg/L is applied to the existing drinking water treatment method to purify the polluted water body, the technical problem is that the concentration requirement of trivalent antimony in water cannot be met in the Hygienic Standard for Drinking Water. The method is as follows: add ferric iron to the water body Salt first enters the flocculation reaction tank and then is filtered by the ultrafiltration tank. The purification method saves costs and is easy to operate. After treatment, the concentration of trivalent antimony in the factory water can be reduced to 1~3μg/L, and the effect is remarkable. It can be used as an emergency treatment plan for ultrafiltration membrane water plants or small rural water plants.
Description
技术领域technical field
本发明涉及一种饮用水突发性污染净化处理方法，具体涉及一种三价铁盐混凝预处理联合超滤短流程工艺去除水中三价锑的方法。The invention relates to a purification treatment method for sudden pollution of drinking water, in particular to a method for removing trivalent antimony in water by coagulation pretreatment of ferric salt combined with a short ultrafiltration process.
背景技术Background technique
锑（Sb）在水环境中以溶解态（Sb3+，Sb5+）或颗粒物的形式存在，三价锑的毒性是五价锑毒性的10倍以上，Sb的主要工业用途有灭火延迟添加剂，制陶等工业用途，Sb不是人体必需元素，并且Sb及其化合物能与人体内巯基结合，干扰体内酶活性或破坏细胞内离子平衡使细胞缺氧而引起人体代谢紊乱，因此《生活饮用水卫生标准》（GB5749-2006）要求生活饮用水中Sb的浓度为低于5μg/L。Antimony (Sb) exists in the form of dissolved (Sb 3+ , Sb 5+ ) or particles in the water environment. The toxicity of trivalent antimony is more than 10 times that of pentavalent antimony. The main industrial use of Sb is fire extinguishing delay additive , pottery and other industrial purposes, Sb is not an essential element for the human body, and Sb and its compounds can combine with sulfhydryl groups in the human body, interfere with the enzyme activity in the body or destroy the ion balance in the cell, causing the cell to be hypoxic and causing metabolic disorders in the human body. Therefore, "Drinking Water Sanitary Standards (GB5749-2006) require the concentration of Sb in drinking water to be less than 5 μg/L.
目前比较成熟的除Sb技术有吸附、沉淀/共沉淀、氧化还原、离子交换等，其中吸附法以其操作简单的优点而应用最为广泛，但这些方法主要是针对废水处理的。这些技术在大规模水厂发生突发性污染时应用有一定困难，主要在于时效性差，短期内很难实施应用。超滤膜技术由于具有高效截留颗粒物、胶体、藻类以及病原性微生物的能力，同时，浸没式膜技术具有易于固液分离，易于操作运行，占地小，且有低压运行耗能低等特点，是目前在国内大型水厂以及农村小型水厂净化处理引用水主要方法，然而面对突发性水体污染，尤其在对水体中三价锑的污染浓度达30~150μg/L的饮用水进行净化处理时，超滤膜水厂需要有应对此突发性污染的技术储备，从而保证出厂水中三价锑的浓度要求达到《生活饮用水卫生标准》。At present, the relatively mature Sb removal technologies include adsorption, precipitation/co-precipitation, redox, ion exchange, etc. Among them, the adsorption method is the most widely used because of its simple operation, but these methods are mainly for wastewater treatment. These technologies are difficult to apply when sudden pollution occurs in large-scale water plants, mainly due to poor timeliness and difficulty in implementing them in a short period of time. Ultrafiltration membrane technology has the ability to efficiently intercept particles, colloids, algae and pathogenic microorganisms. At the same time, submerged membrane technology has the characteristics of easy solid-liquid separation, easy operation, small footprint, and low energy consumption at low pressure. It is currently the main method for purifying drinking water in domestic large-scale water plants and small rural water plants. However, in the face of sudden water pollution, especially for drinking water with a concentration of trivalent antimony in the water of 30-150 μg/L During the treatment, the ultrafiltration membrane water plant needs to have technical reserves to deal with the sudden pollution, so as to ensure that the concentration of trivalent antimony in the discharged water meets the "Drinking Water Hygienic Standard".
发明内容Contents of the invention
本发明是为解决现有饮用水处理方法不适用于突发性的水源水三价锑污染，尤其当水源水中三价锑浓度达30~150μg/L时应用现有饮用水处理方法对污染水体进行净化处理后不能达到《生活饮用水卫生标准》对水中三价锑的浓度要求的技术问题，而提供一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法。The present invention aims to solve the problem that the existing drinking water treatment method is not suitable for the sudden trivalent antimony pollution of water source water, especially when the trivalent antimony concentration in the water source water reaches 30-150 μg/L, the existing drinking water treatment method is applied to the polluted water body After the purification treatment, the technical problem of the concentration of trivalent antimony in the water cannot be met in the "Drinking Water Sanitation Standard", and a short-process process of ferric salt coagulation pretreatment combined with ultrafiltration is provided to remove trivalent antimony in water source water. method.
本发明的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法按以下步骤进行：A method for removing trivalent antimony in water source water according to the present invention is carried out in the following steps:
一、调节原水pH至8~9，然后以水体中三价铁盐的摩尔浓度为0.1~0.8mmol/L向水体中加入三价铁盐，混合1~2min后进入絮凝反应池，反应时间为15~20min；1. Adjust the pH of the raw water to 8~9, then add ferric salt into the water body with the molar concentration of ferric salt in the water body at 0.1~0.8mmol/L, mix for 1~2min and then enter the flocculation reaction tank. The reaction time is 15~20min;
二、经步骤一处理后的水进入超滤膜池过滤，超滤膜通量为20~30L·m-2·h-1，其中超滤膜每过滤8~12h后进行一次气水反冲洗操作，气水反冲洗超滤膜的时间为1~2min，水洗强度为40~60L/(m2·h)，气洗强度为40~60m3/(m2·h)，排污后进入下一个过滤周期；2. The water treated in step 1 enters the ultrafiltration membrane tank for filtration. The flux of the ultrafiltration membrane is 20~30L·m -2 ·h -1 , and the ultrafiltration membrane is backwashed with air and water every 8~12h after filtration. Operation, the air-water backwash ultrafiltration membrane time is 1~2min, the water washing intensity is 40~60L/(m 2 ·h), the air washing intensity is 40~60m 3 /(m 2 ·h), and enters the next a filter cycle;
三、调节步骤二后的出水pH至6.5~8.5，出水至清水池。3. Adjust the pH of the effluent after step 2 to 6.5~8.5, and discharge the water to the clear water pool.
本发明的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，在投加三价铁盐之前调节原水pH值有利于大量三价铁盐水解，使三价铁盐充分与水体中溶解性Sb通过结晶共沉淀作用形成颗粒物质，颗粒物质经超滤膜截留过滤，出水再调节pH值，通过控制三价铁盐的加入量，使得处理后的出厂水中三价锑的浓度低于5μg/L，溶解性铁含量低于0.3mg/L，满足《生活饮用水卫生标准》要求，且投加化学药剂预处理的方式，节省成本，操作方便，不必额外增加基建设施，处理效果显著，可使污染水体中三价锑的浓度降低至1~3μg/L，便于工程化推广应用，可作为超滤膜水厂或农村小型水厂应急处理方案。According to the present invention, a ferric salt coagulation pretreatment combined with an ultrafiltration short-flow process to remove trivalent antimony in water source water adjusts the pH value of raw water before adding ferric salt, which is conducive to the hydrolysis of a large amount of ferric salt, so that The trivalent iron salt fully interacts with the soluble Sb in the water to form particulate matter through crystallization and co-precipitation. The particulate matter is intercepted and filtered by the ultrafiltration membrane, and the pH value of the effluent is adjusted. By controlling the amount of ferric salt added, the treated product leaves the factory The concentration of trivalent antimony in the water is lower than 5μg/L, and the content of soluble iron is lower than 0.3mg/L, which meets the requirements of the "Drinking Water Hygienic Standard", and the method of adding chemical agents for pretreatment saves costs and is easy to operate. Additional infrastructure facilities are added, and the treatment effect is remarkable, which can reduce the concentration of trivalent antimony in polluted water to 1~3μg/L, which is convenient for engineering promotion and application, and can be used as an emergency treatment plan for ultrafiltration membrane water plants or small rural water plants.
附图说明Description of drawings
图1为实施例1~实施例4的原水中三价锑含量与经过实施例1~实施例4的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法处理后的出水中三价锑含量的关系曲线图；Figure 1 shows the content of trivalent antimony in the raw water of Examples 1 to 4 and the results of trivalent antimony in the source water after a short process of ferric salt coagulation pretreatment combined with ultrafiltration in Examples 1 to 4 The relationship curve diagram of the content of trivalent antimony in the effluent after the method is processed;
图2为实施例5~实施例8的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法处理后出水进行水中三价锑含量与FeCl3不同投加量的关系曲线图。Fig. 2 is a method of removing trivalent antimony in source water by a ferric salt coagulation pretreatment combined with ultrafiltration short-flow process of embodiment 5 to embodiment 8. After treatment, the content of trivalent antimony in water and FeCl3 in the effluent are treated differently. Quantitative relationship graph.
具体实施方式Detailed ways
本发明的技术方案不局限于以下具体实施方式，还包括各具体实施方式间的任意组合。The technical solution of the present invention is not limited to the following specific embodiments, but also includes any combination of the specific embodiments.
具体实施方式一：本实施方式的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法按以下步骤进行：Specific implementation mode one: a method for removing trivalent antimony in water source water according to the following steps:
一、调节原水pH至8~9，然后以水体中三价铁盐的摩尔浓度为0.1~0.8mmol/L向水体中加入三价铁盐，混合1~2min后进入絮凝反应池，反应时间为15~20min；1. Adjust the pH of the raw water to 8~9, then add ferric salt into the water body with the molar concentration of ferric salt in the water body at 0.1~0.8mmol/L, mix for 1~2min and then enter the flocculation reaction tank. The reaction time is 15~20min;
二、经步骤一处理后的水进入超滤膜池过滤，超滤膜通量为20~30L·m-2·h-1，其中超滤膜每过滤8~12h后进行一次气水反冲洗操作，气水反冲洗超滤膜的时间为1~2min，水洗强度为40~60L/(m2·h)，气洗强度为40~60m3/(m2·h)，排污后进入下一个过滤周期；2. The water treated in step 1 enters the ultrafiltration membrane tank for filtration. The flux of the ultrafiltration membrane is 20~30L·m -2 ·h -1 , and the ultrafiltration membrane is backwashed with air and water every 8~12h after filtration. Operation, the air-water backwash ultrafiltration membrane time is 1~2min, the water washing intensity is 40~60L/(m 2 ·h), the air washing intensity is 40~60m 3 /(m 2 ·h), and enters the next a filter cycle;
三、调节步骤二后的出水pH至6.5~8.5，出水至清水池。3. Adjust the pH of the effluent after step 2 to 6.5~8.5, and discharge the water to the clear water pool.
本实施方式的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，在投加三价铁盐之前调节原水pH值有利于大量三价铁盐水解，使三价铁盐充分与水体中溶解性Sb通过结晶共沉淀作用形成颗粒物质，颗粒物质经超滤膜截留过滤，出水再调节pH值，通过控制三价铁盐的加入量，使得处理后的出厂水中三价锑的浓度低于5μg/L，溶解性铁含量低于0.3mg/L，满足《生活饮用水卫生标准》要求，且投加化学药剂预处理的方式，节省成本，操作方便，不必额外增加基建设施，处理效果显著，可使污染水体中三价锑的浓度降低至1~3μg/L，便于工程化推广应用，可作为超滤膜水厂或农村小型水厂应急处理方案。In this embodiment, a ferric salt coagulation pretreatment combined with an ultrafiltration short-flow process to remove trivalent antimony in water source water adjusts the pH value of the raw water before adding ferric salt, which is conducive to the hydrolysis of a large amount of ferric salt. The trivalent iron salt is fully combined with the soluble Sb in the water to form particulate matter through crystallization and co-precipitation. The particulate matter is intercepted and filtered by the ultrafiltration membrane, and the pH value of the effluent is adjusted. By controlling the amount of ferric salt added, the treated The concentration of trivalent antimony in the factory water is lower than 5μg/L, and the content of soluble iron is lower than 0.3mg/L, which meets the requirements of the "Drinking Water Hygienic Standard", and the method of adding chemical agents for pretreatment saves costs and is easy to operate. There is no need to add additional infrastructure facilities, and the treatment effect is remarkable. It can reduce the concentration of trivalent antimony in polluted water to 1~3μg/L, which is convenient for engineering promotion and application. It can be used as an emergency treatment plan for ultrafiltration membrane water plants or small rural water plants.
具体实施方式二：本实施方式与具体实施方式一不同的是：步骤一和步骤三中调节pH的药剂为烧碱溶液或碱石灰溶液，其它步骤与参数与具体实施方式一相同。Embodiment 2: The difference between this embodiment and Embodiment 1 is that the agent for adjusting pH in Step 1 and Step 3 is caustic soda solution or soda lime solution, and other steps and parameters are the same as Embodiment 1.
具体实施方式三：本实施方式与具体实施方式一或二不同的是：步骤一中加入三价铁盐的量为0.4mmol/L，其它步骤与参数与具体实施方式一或二相同。Embodiment 3: The difference between this embodiment and Embodiment 1 or 2 is that the amount of ferric salt added in Step 1 is 0.4 mmol/L, and other steps and parameters are the same as Embodiment 1 or 2.
具体实施方式四：本实施方式与具体实施方式一至三之一不同的是：步骤二中超滤膜池所用超滤膜材质为聚氯乙烯，其它步骤与参数与具体实施方式一至三之一相同。Embodiment 4: This embodiment differs from Embodiment 1 to Embodiment 3 in that the material of the ultrafiltration membrane used in the ultrafiltration membrane pool in step 2 is polyvinyl chloride, and other steps and parameters are the same as Embodiment 1 to Embodiment 3. .
具体实施方式五：本实施方式与具体实施方式一至四之一不同的是：步骤二中超滤膜池所用超滤膜公称孔径为0.01μm，其它步骤与参数与具体实施方式一至四之一相同。Embodiment 5: This embodiment differs from Embodiment 1 to Embodiment 4 in that: the nominal pore size of the ultrafiltration membrane used in the ultrafiltration membrane pool in step 2 is 0.01 μm, and other steps and parameters are the same as Embodiment 1 to Embodiment 4. .
用以下试验验证本发明的有益效果：Verify beneficial effect of the present invention with following test:
实施例1、一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法按以下步骤进行：Embodiment 1. A method for removing trivalent antimony in water source water by coagulation pretreatment of ferric salt combined with ultrafiltration short process is carried out in the following steps:
一、向三价锑的质量浓度为30μg/L的原水中，通过计量泵送入烧碱溶液将水体PH均调节至PH为8.8，然后用柱塞隔膜泵以水体中Fe3+的摩尔浓度为0.4mmol/L向水体中加入FeCl3，混合1min后进入絮凝反应池，反应20min；1. Send the caustic soda solution into the raw water with the mass concentration of trivalent antimony of 30 μg/L to adjust the pH of the water body to 8.8, and then use the plunger diaphragm pump to set the molar concentration of Fe in the water body as Add 0.4mmol/L FeCl 3 to the water body, mix for 1min, enter the flocculation reaction tank, and react for 20min;
二、经步骤一处理后的水进入超滤膜池过滤，超滤膜通量为30L·m-2·h-1，过滤10h后，气水反冲洗超滤膜2min，水洗强度为60L/(m2·h)，气洗强度为50m3/(m2·h)，超滤膜公称孔径为0.01μm，排污后进入下一个过滤周期，循环三次；2. The water treated in step 1 enters the ultrafiltration membrane tank for filtration. The flux of the ultrafiltration membrane is 30L·m -2 ·h -1 . After 10 hours of filtration, the air and water backwash the ultrafiltration membrane for 2 minutes, and the washing strength is 60L/ (m 2 ·h), the air washing intensity is 50m 3 /(m 2 ·h), the nominal pore size of the ultrafiltration membrane is 0.01μm, after the sewage is discharged, it enters the next filtration cycle and cycles three times;
三、调节步骤二后的出水PH为7，出水至清水池。3. Adjust the PH of the effluent after step 2 to 7, and effluent to the clear water pool.
实施例2、一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，本实施例与实施例1不同的是原水中三价锑的质量浓度为54μg/L，其他步骤及参数与实施例1相同。Embodiment 2. A method for removing trivalent antimony in source water by coagulation pretreatment of ferric salt combined with ultrafiltration short-flow process. The difference between this embodiment and embodiment 1 is that the mass concentration of trivalent antimony in raw water is 54 μg/ L, other steps and parameters are the same as in Example 1.
实施例3、一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，本实施例与实施例1不同的是原水中三价锑的质量浓度为124μg/L，其他步骤及参数与实施例1相同。Embodiment 3, a method for removing trivalent antimony in water source water by coagulation pretreatment of ferric salt combined with ultrafiltration short process, the difference between this embodiment and embodiment 1 is that the mass concentration of trivalent antimony in raw water is 124 μg/ L, other steps and parameters are the same as in Example 1.
实施例4、一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，本实施例与实施例1不同的是原水中三价锑的质量浓度为148μg/L，其他步骤及参数与实施例1相同。Embodiment 4, a method for removing trivalent antimony in water source water by coagulation pretreatment of ferric salt combined with ultrafiltration short-flow process, the difference between this embodiment and embodiment 1 is that the mass concentration of trivalent antimony in raw water is 148 μg/ L, other steps and parameters are the same as in Example 1.
实施例5、一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法按以下步骤进行：Embodiment 5, a method for removing trivalent antimony in water source water by coagulation pretreatment of ferric salt combined with ultrafiltration short-flow process is carried out according to the following steps:
一、向三价锑的质量浓度为85μg/L的原水中，通过计量泵送入烧碱溶液将水体PH调节至PH为9.0，然后用柱塞隔膜泵以水体中Fe3+的摩尔浓度为0.1mmol/L向水体中加入FeCl3，混合1min后转入絮凝反应池，反应20min；1. To the raw water with the mass concentration of trivalent antimony of 85 μg/L, send caustic soda solution through metering pump to adjust the pH of the water body to 9.0, and then use the plunger diaphragm pump to set the molar concentration of Fe 3+ in the water body to 0.1 Add FeCl 3 to the water body in mmol/L, mix for 1 minute, transfer to the flocculation reaction tank, and react for 20 minutes;
二、经步骤一处理后的水体进入超滤膜池过滤，超滤膜通量为30L·m-2·h-1，过滤10h后，气水反冲洗超滤膜2min，水洗强度为60L/(m2·h)，气洗强度为50m3/(m2·h)，超滤膜公称孔径为0.01μm，排污后进入下一个过滤周期，循环三次；2. The water treated in step 1 enters the ultrafiltration membrane tank for filtration. The flux of the ultrafiltration membrane is 30L·m -2 ·h -1 . After 10 hours of filtration, the air and water backwash the ultrafiltration membrane for 2 minutes, and the washing strength is 60L/ (m 2 ·h), the air washing intensity is 50m 3 /(m 2 ·h), the nominal pore size of the ultrafiltration membrane is 0.01μm, after the sewage is discharged, it enters the next filtration cycle and cycles three times;
三、调节步骤二后的出水PH为7.0，出水至清水池。3. Adjust the pH of the effluent after step 2 to 7.0, and effluent to the clear water pool.
实施例6、一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，本实施例与实施例5不同的是水体中FeCl3的投加量按水体中Fe3+的摩尔浓度为0.2mmol/L添加，其他步骤及参数与实施例5相同。Embodiment 6, a method for ferric salt coagulation pretreatment combined with ultrafiltration short flow process to remove trivalent antimony in water source water, the difference between this embodiment and embodiment 5 is that the dosage of FeCl in the water body is the same as in the water body The molar concentration of Fe 3+ was added at 0.2mmol/L, and other steps and parameters were the same as in Example 5.
实施例7、一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，本实施例与实施例5不同的是水体中FeCl3的投加量按水体中Fe3+的摩尔浓度为0.4mmol/L添加，其他步骤及参数与实施例5相同。Embodiment 7, a method for ferric salt coagulation pretreatment combined with ultrafiltration short flow process to remove trivalent antimony in water source water. The difference between this embodiment and embodiment 5 is that the dosage of FeCl in the water body is the same as in the water body The molar concentration of Fe 3+ was added at 0.4mmol/L, and other steps and parameters were the same as in Example 5.
实施例8、一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法，本实施例与实施例5不同的是水体中FeCl3的投加量按水体中Fe3+的摩尔浓度为0.8mmol/L添加，其他步骤及参数与实施例5相同。Embodiment 8, a method for ferric salt coagulation pretreatment combined with ultrafiltration short flow process to remove trivalent antimony in water source water, the difference between this embodiment and embodiment 5 is that the dosage of FeCl3 in the water body is the same as in the water body The molar concentration of Fe 3+ was added at 0.8mmol/L, and other steps and parameters were the same as in Example 5.
试验一、对经过实施例1～实施例4的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法处理后的出水进行水中三价锑含量检测试验：Test 1. The trivalent antimony content detection test in water was carried out on the effluent treated by the method of removing trivalent antimony in water source water through a kind of ferric salt coagulation pretreatment combined with ultrafiltration short process process of embodiment 1 to embodiment 4:
根据《生活饮用水卫生标准》（GB5749-2006），采用《生活饮用水标准检验方法》（GB5750-2006），对经过实施例1~实施例4的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法处理后的出水进行水中三价锑含量检测，得到如图1所示的曲线图，从图中可以看出，当原水中三价锑质量浓度为30μg/L时，出水中三价锑质量浓度为1.1μg/L，当原水中三价锑质量浓度为148μg/L时，出水中三价锑质量浓度也仅为2.8μg/L，处理效果好，处理后的出水符合《生活饮用水卫生标准》要求，可用于超滤膜水厂或农村小型水厂放生突发性三价锑污染。According to the "Drinking Water Hygienic Standard" (GB5749-2006), using the "Drinking Water Standard Test Method" (GB5750-2006), a combination of ferric salt coagulation pretreatment through Example 1~Example 4 The method of removing trivalent antimony in water source water by ultrafiltration short process process The treated effluent is tested for trivalent antimony content in water, and the curve shown in Figure 1 is obtained. It can be seen from the figure that when the mass concentration of trivalent antimony in raw water When the mass concentration of trivalent antimony in the effluent is 30 μg/L, the mass concentration of trivalent antimony in the effluent is 1.1 μg/L. When the mass concentration of trivalent antimony in the raw water is 148 μg/L, the mass concentration of trivalent antimony in the effluent is only 2.8 μg/L. The treatment effect Well, the treated effluent meets the requirements of the Sanitary Standard for Drinking Water and can be used in ultrafiltration membrane water plants or small rural water plants to release sudden trivalent antimony pollution.
试验二、对经过实施例5~实施例8的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法处理后的出水进行水中三价铁含量检测试验：Test 2. The effluent treated by the method of removing trivalent antimony in water source water by a kind of ferric salt coagulation pretreatment combined with ultrafiltration short flow process of embodiment 5 to embodiment 8 is tested for ferric iron content in water:
根据《生活饮用水卫生标准》（GB5749-2006），采用《生活饮用水标准检验方法》（GB5750-2006），对经过实施例5~实施例8的一种三价铁盐混凝预处理联合超滤短流程工艺去除水源水中三价锑的方法处理后出水进行水中三价锑含量检测，得到如图2所示的FeCl3不同投加量与出水中三价锑含量的关系曲线图，从图中可以看出，当以水体中Fe3+的摩尔浓度为0.1mmol/L向原水中投加FeCl3处理后，出水中三价锑质量浓度为25μg/L，当以水体中Fe3+的摩尔浓度为0.2mmol/L向原水中投加FeCl3处理后，出水中三价锑质量浓度为16μg/L，当以水体中Fe3+的摩尔浓度为0.4mmol/L向原水中投加FeCl3处理后，出水中三价锑质量浓度为5μg/L，当以水体中Fe3+的摩尔浓度为0.8mmol/L向原水中投加FeCl3处理后，出水中三价锑质量浓度为1μg/L，由图得出，当水体中三价锑的质量浓度为85μg/L时，FeCl3的最佳投放量为0.4~0.8mmol/L，此时出水即可符合《生活饮用水卫生标准》要求。According to the "Drinking Water Hygienic Standard" (GB5749-2006), using the "Drinking Water Standard Test Method" (GB5750-2006), a combination of ferric salt coagulation pretreatment through Example 5~Example 8 The method of removing trivalent antimony in water source water by ultrafiltration short-flow process is used to detect the content of trivalent antimony in the effluent after treatment, and obtain the relationship curve between different dosages of FeCl3 and the content of trivalent antimony in the effluent as shown in Figure 2, from It can be seen from the figure that when the molar concentration of Fe 3+ in the water body is 0.1 mmol/L, FeCl 3 is added to the raw water for treatment, and the mass concentration of trivalent antimony in the effluent is 25 μg/L. When the molar concentration of Fe 3+ in the water body is After adding FeCl 3 to the raw water with a molar concentration of 0.2mmol/L, the mass concentration of trivalent antimony in the effluent water is 16μg/L. Finally, the mass concentration of trivalent antimony in the effluent is 5 μg/L. When FeCl 3 is added to the raw water with the molar concentration of Fe 3+ in the water body as 0.8 mmol/L, the mass concentration of trivalent antimony in the effluent is 1 μg/L. It can be concluded from the figure that when the mass concentration of trivalent antimony in the water body is 85 μg/L, the optimal dosage of FeCl 3 is 0.4~0.8 mmol/L, and the effluent at this time can meet the requirements of the "Drinking Water Sanitation Standard".
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103922512A (en) * | 2014-05-05 | 2014-07-16 | 哈尔滨工业大学 | Method for removing trace antimony in water |
| CN110316870A (en) * | 2019-07-17 | 2019-10-11 | 深圳信息职业技术学院 | A kind of sludge preload flocculation-ultrafiltration membrane two-part effluent purification method |
| CN115043513A (en) * | 2022-04-22 | 2022-09-13 | 锡矿山闪星锑业有限责任公司 | A kind of waste water treatment system containing antimony and arsenic |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63236592A (en) * | 1987-03-26 | 1988-10-03 | Kurita Water Ind Ltd | How to treat antimony-containing water |
| JPH11216356A (en) * | 1998-01-30 | 1999-08-10 | Toagosei Co Ltd | Antimony adsorbent |
| AU4810501A (en) * | 2000-06-01 | 2001-12-06 | Ben-Gurion University Of The Negev Research & Development Authority | Method for treating contaminated liquid |
| US6428705B1 (en) * | 1996-11-26 | 2002-08-06 | Microbar Incorporated | Process and apparatus for high flow and low pressure impurity removal |
| JP4045332B2 (en) * | 1998-03-26 | 2008-02-13 | Ｄｏｗａエコシステム株式会社 | Treatment of wastewater containing Sb |
| CN101428932A (en) * | 2008-12-09 | 2009-05-13 | 中南大学 | Method for treating stibium-containing wastewater with biological agent |
| CN101973651A (en) * | 2010-08-27 | 2011-02-16 | 湖南恒辉膜技术有限公司 | Membrane treatment method for treating trace antimony in drinking water |
| CN202415290U (en) * | 2011-12-22 | 2012-09-05 | 广州市自来水公司 | Emergency treatment system for raw water polluted by antimony |
-
2012
- 2012-12-28 CN CN2012105834655A patent/CN103011461A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63236592A (en) * | 1987-03-26 | 1988-10-03 | Kurita Water Ind Ltd | How to treat antimony-containing water |
| US6428705B1 (en) * | 1996-11-26 | 2002-08-06 | Microbar Incorporated | Process and apparatus for high flow and low pressure impurity removal |
| JPH11216356A (en) * | 1998-01-30 | 1999-08-10 | Toagosei Co Ltd | Antimony adsorbent |
| JP4045332B2 (en) * | 1998-03-26 | 2008-02-13 | Ｄｏｗａエコシステム株式会社 | Treatment of wastewater containing Sb |
| AU4810501A (en) * | 2000-06-01 | 2001-12-06 | Ben-Gurion University Of The Negev Research & Development Authority | Method for treating contaminated liquid |
| CN101428932A (en) * | 2008-12-09 | 2009-05-13 | 中南大学 | Method for treating stibium-containing wastewater with biological agent |
| CN101973651A (en) * | 2010-08-27 | 2011-02-16 | 湖南恒辉膜技术有限公司 | Membrane treatment method for treating trace antimony in drinking water |
| CN202415290U (en) * | 2011-12-22 | 2012-09-05 | 广州市自来水公司 | Emergency treatment system for raw water polluted by antimony |
Non-Patent Citations (2)
| Title |
|---|
| MEEA KANG,TASUKU K,YASUMOTO M: "Comparing polyaluminum chloride and ferric chloride for antimony removl", 《WATER RESEARCH》, vol. 37, no. 17, 31 December 2003 (2003-12-31) * |
| 崔俊华等: "基于在线混凝-超滤组合工艺的微污染地表水处理", 《河北工程大学学报(自然科学版)》, vol. 28, no. 01, 31 March 2011 (2011-03-31) * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103922512A (en) * | 2014-05-05 | 2014-07-16 | 哈尔滨工业大学 | Method for removing trace antimony in water |
| CN110316870A (en) * | 2019-07-17 | 2019-10-11 | 深圳信息职业技术学院 | A kind of sludge preload flocculation-ultrafiltration membrane two-part effluent purification method |
| CN115043513A (en) * | 2022-04-22 | 2022-09-13 | 锡矿山闪星锑业有限责任公司 | A kind of waste water treatment system containing antimony and arsenic |
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