WO2023060986A1 - 一种再生水中痕量小分子有机物的去除方法 - Google Patents

一种再生水中痕量小分子有机物的去除方法 Download PDF

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WO2023060986A1
WO2023060986A1 PCT/CN2022/108485 CN2022108485W WO2023060986A1 WO 2023060986 A1 WO2023060986 A1 WO 2023060986A1 CN 2022108485 W CN2022108485 W CN 2022108485W WO 2023060986 A1 WO2023060986 A1 WO 2023060986A1
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water
concentration
urea
resin column
regenerated
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French (fr)
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熊江磊
陈炜彧
蒋士龙
周伟
袁润博
田宇鸣
蔡宏展
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江苏中电创新环境科技有限公司
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Priority to JP2023557481A priority Critical patent/JP2023554167A/ja
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    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/30—Treatment of water, waste water, or sewage by irradiation
    • C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/422—Treatment of water, waste water, or sewage by ion-exchange using anionic exchangers
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/34—Organic compounds containing oxygen
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/38—Organic compounds containing nitrogen

Definitions

  • the invention relates to a method for removing trace small molecule organic matter in regenerated water.
  • the existing industrial wastewater/sewage plant tail water regeneration treatment process is mainly a combination of ultrafiltration (UF) and reverse osmosis (RO), which can effectively remove most of the total organic carbon (TOC) and total dissolved solids in the wastewater (TDS) and other pollutants, so as to produce higher quality reclaimed water.
  • UF ultrafiltration
  • RO reverse osmosis
  • the TOC concentration of regenerated water treated by UF+RO is very low (generally TOC ⁇ 1mg/L).
  • Reclaimed water can be used for general industrial production, agricultural irrigation, urban landscape, and groundwater replenishment, etc., but for electronics/new energy industries such as integrated circuits, flat panel displays, and new energy that have high requirements for raw water production, recycled water cannot be directly reused.
  • TOC in RO produced water is mostly small molecular organic matter, which is difficult to be effectively removed in the existing ultrapure water preparation system: activated carbon, ion exchange resin, reverse osmosis, TOC-UV and other process units
  • activated carbon ion exchange resin
  • reverse osmosis reverse osmosis
  • TOC-UV reverse osmosis
  • the treatment effect on small molecular organics is limited, and the removal rate is only 10% to 20%. Therefore, small molecular organics in reclaimed water will cause the TOC of ultrapure water system to exceed the standard, which will eventually have a great impact on the yield of electronic products.
  • the small molecule organics in the regenerated water treated by UF+RO are mainly urea, trihalomethanes and other neutral organics with small molecular weight and no charge, among which urea accounts for the largest proportion.
  • the urea concentration in the water is generally 80ppb-120ppb, much higher than the urea concentration in municipal tap water (10ppb-30ppb). Therefore, it is necessary to effectively remove traces of small molecular organics, especially urea, in the regenerated water before it is reused for the preparation of electronic ultrapure water.
  • the lower limit value of organic matter concentration is about 1ppm, while the concentration of small molecule organic matter in reclaimed water is 80ppb-120ppb, which is far lower than the lower limit value of high-concentration organic matter in conventionally treated water bodies.
  • the existing treatment methods for trace small molecular organics in reclaimed water have the problems of complex process, easy to cause other problems and low removal rate.
  • the purpose of the invention is to provide a method for removing trace small molecular organics in regenerated water with simple process and high removal rate.
  • the method for removing traces of small molecular organics in regenerated water according to the present invention is to pass the reverse osmosis regenerated water added with an oxidizing agent into an ultraviolet oxidation device, and oxidize the oxidizing agent and traces of small molecular organics in the regenerated water under the irradiation of ultraviolet light Reduction reaction; wherein, the oxidizing agent includes the following components in mass fraction: 6.0%-7.0% hydrogen peroxide, 40.0%-42.0% peroxodisulfate, 2.0%-3.0% chloramine and 48.0%-50.0% water.
  • reaction time is 30-300s. The fuller the reaction time, the better the removal effect.
  • the total concentration of active ingredients is positively correlated with the removal effect. The higher the total concentration of active ingredients within a certain range, the better the removal effect.
  • Ultraviolet light acts as a catalyst in the reaction, and a sufficient dose of ultraviolet light can ensure that the oxidant is fully decomposed to generate free radicals in a short period of time, thereby achieving a better catalytic effect.
  • the reclaimed water is obtained by the following method: the collected tail water of the sewage plant passes through a multimedia filter, a security filter, an ultrafiltration device and a reverse osmosis device in order to obtain the regenerated water.
  • the product water after the oxidation-reduction reaction is passed into the resin column, and the concentration of urea in the product water after the oxidation-reduction reaction is obtained through conversion by detecting the TOC concentration of the effluent from the resin column.
  • the resin column is filled with strong acid cation exchange resin and strong base anion exchange resin.
  • the oxidant of the present invention is different from the traditional single oxidant in removing urea, and overcomes the shortcomings of the traditional single oxidant such as low free radical generation and long reaction time.
  • the three oxidants excite each other to generate a large number of free radicals.
  • free radicals with strong oxidizing ability sulfate radicals, hydroxyl radicals, and chlorine free radicals, the three free radicals cooperate to redox urea in situ.
  • the present invention has the following significant advantages: the removal method of the present invention is simple in process, can effectively remove trace urea in reclaimed water, and can make the regenerated water with an initial concentration of urea between 60ppb and 125ppb The concentration of urea is reduced to 5ppb, so that the regenerated water can be reused for the preparation of electronic ultrapure water.
  • Figure 1 is a graph showing the relationship between the concentration of urea in water and the concentration of TOC in water.
  • the regenerated water obtained after UF+RO treatment is added with an oxidant and then passed into the ultraviolet oxidation device.
  • the ultraviolet lamp is installed in the ultraviolet oxidation device, and the regenerated water with the oxidant is irradiated through the ultraviolet lamp.
  • the oxidant includes the following mass fractions: Divide: 6.0% hydrogen peroxide, 42.0% peroxodisulfate, 2.0% chloramine and 50.0% water.
  • the concentration of urea in reclaimed water is 123ppb;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the TOC concentration of the effluent from the resin column is 6.9ppb, and the urea concentration is 27ppb; the urea removal rate is 78.05%.
  • the regenerated water obtained after UF+RO treatment is added with an oxidant and then passed into the ultraviolet oxidation device.
  • the ultraviolet lamp is installed in the ultraviolet oxidation device, and the regenerated water with the oxidant is irradiated through the ultraviolet lamp.
  • the oxidant includes the following mass fractions: Divide: 6.0% hydrogen peroxide, 42.0% peroxodisulfate, 2.0% chloramine and 50.0% water.
  • the concentration of urea in reclaimed water is 83ppb;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the TOC concentration of the resin column effluent is 3.7ppb, and the urea concentration is 13ppb; the urea removal rate is 84.34%.
  • the regenerated water obtained after UF+RO treatment is added with an oxidant and then passed into the ultraviolet oxidation device.
  • the ultraviolet lamp is installed in the ultraviolet oxidation device, and the regenerated water with the oxidant is irradiated through the ultraviolet lamp.
  • the oxidant includes the following mass fractions: Divide: 6.0% hydrogen peroxide, 42.0% peroxodisulfate, 2.0% chloramine and 50.0% water.
  • the concentration of urea in reclaimed water is 68ppb;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the TOC concentration of the resin column effluent is 2.9ppb, and the urea concentration is 8ppb; the urea removal rate is 88.24%.
  • the formula has guiding significance.
  • the regenerated water obtained after UF+RO treatment is added with an oxidant and then passed into the ultraviolet oxidation device.
  • the ultraviolet lamp is installed in the ultraviolet oxidation device, and the regenerated water with the oxidant is irradiated through the ultraviolet lamp.
  • the oxidant includes the following mass fractions: Divide: 7.0% hydrogen peroxide, 40.0% peroxodisulfate, 3.0% chloramine and 50.0% water.
  • the concentration of urea in reclaimed water is 68ppb;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the TOC concentration of the product water was 10.1ppb.
  • the TOC concentration of the resin column effluent is 3.0pb, and the urea concentration is 9ppb; the urea removal rate is 86.76%.
  • the formula has guiding significance.
  • the regenerated water obtained after UF+RO treatment is added with an oxidant and then passed into the ultraviolet oxidation device.
  • the ultraviolet lamp is installed in the ultraviolet oxidation device, and the regenerated water with the oxidant is irradiated through the ultraviolet lamp.
  • the oxidant includes the following mass fractions: Divide: 6.0% hydrogen peroxide, 42.0% peroxodisulfate, 2.0% chloramine and 50.0% water.
  • the concentration of urea in reclaimed water is 123ppb;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • Example 1 Pass the product water into the resin column. After testing, the TOC concentration of the effluent from the resin column is 11.2pb, and the urea concentration is 48ppb; the urea removal rate is 60.98%, which is 17.07% lower than that of Example 1. It can be seen from Example 1 and Comparative Example 1 that when the amount of oxidant added is not enough, a good urea removal effect cannot be achieved.
  • the concentration of urea in reclaimed water is 123ppb;
  • the amount of hydrogen peroxide added is 30ppm (30ppm refers to the concentration of hydrogen peroxide in the mixture);
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the irradiation dose is 160mJ/cm 2 ;
  • the concentration of urea in reclaimed water is 123ppb;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the irradiation dose is 160mJ/cm 2 ;
  • the regenerated water obtained after UF+RO treatment is added with permonosulfate and then passed into the ultraviolet oxidation device.
  • the ultraviolet lamp is installed in the ultraviolet oxidizer, and the regenerated water added with peroxysulfate is irradiated through the ultraviolet lamp.
  • the concentration of urea in reclaimed water is 123ppb;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the irradiation dose is 160mJ/cm 2 ;
  • the urea concentration in the resin column effluent is 108ppb, and the urea removal rate is 12.2%.
  • the concentration of urea in reclaimed water is 123ppb;
  • the addition amount of chloramine is 30ppm;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the irradiation dose is 160mJ/cm 2 ;
  • the urea concentration in the resin column effluent is 110ppb, and the urea removal rate is 10.6%.
  • the mixed solution of hydrogen peroxide and peroxodisulfate to the regenerated water obtained after UF+RO treatment, and then pass it into the ultraviolet oxidation device.
  • the ultraviolet lamp is installed in the ultraviolet oxidation device, and the mixed solution is added to the mixed solution through the ultraviolet lamp.
  • the regenerated water is irradiated, and the mixed solution includes the following components in mass fractions: 6.0% hydrogen peroxide, 42.0% peroxodisulfate and 52.0% water.
  • the concentration of urea in reclaimed water is 123ppb;
  • the total addition of hydrogen peroxide and disulfate is 30ppm;
  • the hydraulic retention time in the UV oxidation device is 120s;
  • the irradiation dose is 160mJ/cm 2 ;
  • Example 1 and Comparative Examples 2 to 6 it can be seen that for the removal of trace urea in regenerated water, neither a single oxidant nor coupling of two oxidants can achieve the removal effect of the oxidant of the present invention.
  • the specific reason is related to the molecular structure of urea itself on the one hand.
  • it is also related to the single oxidant itself and the amount and oxidative capacity of the free radicals produced.
  • Multiple oxidants can synergistically stimulate each other to generate more free radicals that react with urea.
  • the oxidizing agent of the present invention can generate electrophilic free radicals with strong oxidizing ability aiming at the molecular structure of urea itself, so as to realize efficient removal of urea in regenerated water.

Abstract

本发明公开了一种再生水中痕量小分子有机物的去除方法，所述方法为：将添加有氧化剂的反渗透再生水通入紫外氧化装置中，在紫外光照射下氧化剂与再生水中痕量小分子有机物发生氧化还原反应；其中，氧化剂包括如下质量分数的组分：6.0％～7.0％双氧水、40.0％～42.0％过二硫酸盐、2.0％～3.0％氯胺和48.0％～50.0％水。本发明的去除方法工艺简单，能够有效去除再生水中痕量尿素，针对尿素初始浓度为60ppb～125ppb的再生水，能够使产水中尿素浓度降低到5ppb，从而实现再生水回用于电子超纯水的制备。

Description

一种再生水中痕量小分子有机物的去除方法 技术领域
本发明涉及一种再生水中痕量小分子有机物的去除方法。
背景技术
现有工业废水/污水厂尾水再生处理工艺主要为超滤(UF)和反渗透(RO)相结合的方式，该方式可有效去除废水中的大部分总有机碳(TOC)、总溶解固体(TDS)等污染物，从而产出较高品质的再生水。经UF+RO处理的再生水TOC浓度很低(一般TOC＜1mg/L)。再生水可用于一般工业生产、农业灌溉、城市景观以及地下水补充等，但对于集成电路、平板显示、新能源等对生产原水要求较高的电子/新能源等行业来说，再生水无法直接回用于电子超纯水的制备，主要是因为RO产水的TOC多为小分子有机物，在现有超纯水制备系统中难以得到有效去除：活性炭、离子交换树脂、反渗透、TOC-UV等工艺单元对小分子有机物的处理作用有限，去除率仅为10％～20％，因此再生水中的小分子有机物将导致超纯水系统产水TOC超标，最终会对电子产品良率造成较大影响。
经UF+RO处理后的再生水中小分子有机物主要为尿素、三卤甲烷等分子量小、不带电荷的中性有机物，其中以尿素占比最大。典型市政污水厂尾水经反渗透后，水中尿素浓度一般为80ppb～120ppb，远高于市政自来水中的尿素浓度(10ppb～30ppb)。因此需要在再生水回用于电子超纯水制备之前就将再生水中的痕量小分子有机物，尤其是尿素进行有效去除。大多数降解水体中有机物的方法对于有机物浓度处理下限值是有机物浓度为1ppm左右，而再生水中小分子有机物浓度为80ppb～120ppb，远远低于常规处理水体中高浓度有机物的处理下限值。现有再生水中痕量小分子有机物的处理方法存在工艺复杂、易引发其他问题以及去除率低的问题。
发明内容
发明目的：本发明的目的是提供一种工艺简单、去除率高的再生水中痕量小分子有机物的去除方法。
技术方案：本发明所述的再生水中痕量小分子有机物的去除方法，将添加有氧化剂的反渗透再生水通入紫外氧化装置中，在紫外光照射下氧化剂与再生水中痕量小分子有机物发生氧化还原反应；其中，氧化剂包括如下质量分数的组分：6.0％～7.0％双氧水、40.0％～42.0％过二硫酸盐、2.0％～3.0％氯胺和48.0％～50.0％水。
其中，反应时间为30～300s。反应时间越充分，去除效果越好。
其中，氧化剂有效成分浓度与再生水中尿素浓度的关系式为：Y＝5.1ln(X)+2.9，X 为再生水中尿素浓度，单位ppb；Y为氧化剂中有效成分总浓度，单位ppm。有效成分总浓度与去除效果正相关，在一定范围内有效成分总浓度越高，去除效果越好。
其中，紫外光照射剂量与再生水中尿素浓度的关系式为：Z＝3.4X 0.8；式中，X为再生水中尿素浓度，单位ppb；Z为紫外光照射剂量，单位mJ/cm 2。紫外光在反应中起催化剂作用，足够照射剂量的紫外光才能保证在短时间内氧化剂充分分解产生自由基，从而实现更好的催化效果。
其中，所述再生水采用如下方法得到：将收集的污水厂尾水依次通过多介质过滤器、保安过滤器、超滤装置和反渗透装置，得到再生水。
其中，将氧化还原反应后的产水通入树脂柱中，通过检测树脂柱出水的TOC浓度，经换算得到氧化还原反应后产水中的尿素浓度。树脂柱出水TOC浓度与氧化还原反应后产水中尿素浓度的关系式为：W＝0.2X+1.3；式中，X为氧化还原反应后产水中尿素浓度，单位ppb；W为树脂柱出水TOC浓度，单位ppb。
其中，所述树脂柱内填充有强酸阳离子交换树脂和强碱阴离子交换树脂。
本发明氧化剂与传统单一氧化剂去除尿素的方式不同，克服了传统单一氧化剂自由基产生量低、反应时间长的缺点，通过紫外光的催化作用，三个氧化剂彼此激发产生大量的自由基，且均为具有强氧化能力自由基，硫酸根自由基、羟基自由基、氯自由基，三个自由基原位协同氧化还原尿素。
有益效果：相比于现有技术，本发明具备的显著优点为：本发明的去除方法工艺简单，能够有效去除再生水中痕量尿素，针对尿素初始浓度为60ppb～125ppb的再生水，能够使产水中尿素浓度降低到5ppb，从而实现再生水回用于电子超纯水的制备。
附图说明
图1为水体中尿素浓度与水体TOC浓度的关系图。
具体实施方式
实施例1
将经过UF+RO处理后得到的再生水投加氧化剂后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有氧化剂的再生水进行照射，氧化剂包括如下质量分数的组分：6.0％双氧水、42.0％过二硫酸盐、2.0％氯胺和50.0％水。
再生水中尿素浓度为123ppb；
氧化剂的加入量为Y＝5.1ln(123)+2.9＝27.4ppm，取30ppm(30ppm是指氧化剂中三个有效成分-双氧水、过二硫酸盐和氯胺的总浓度)；
紫外氧化装置中水力停留时间为120s；
照射剂量为Z＝3.4(123) 0.8＝159.7mJ/cm 2，取160mJ/cm 2；
经检测，产水TOC浓度为16.8ppb。
将产水通入树脂柱，经检测，树脂柱出水的TOC浓度为6.9ppb，尿素浓度为27ppb；尿素去除率为78.05％。经换算，产水中尿素含量X＝(6.9-1.3)/0.2＝28ppb，极差为1，相对偏差3.7％，公式具有指导意义。
实施例2
将经过UF+RO处理后得到的再生水投加氧化剂后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有氧化剂的再生水进行照射，氧化剂包括如下质量分数的组分：6.0％双氧水、42.0％过二硫酸盐、2.0％氯胺和50.0％水。
再生水中尿素浓度为83ppb；
氧化剂的加入量为Y＝5.1ln(83)+2.9＝25.4ppm，取25ppm；
紫外氧化装置中水力停留时间为120s；
照射剂量为Z＝3.4(83) 0.8＝116.6mJ/cm 2，取119mJ/cm 2；
经检测，产水TOC浓度为10.9ppb。
将产水通入树脂柱，经检测，树脂柱出水的TOC浓度为3.7ppb，尿素浓度为13ppb；尿素去除率为84.34％。经换算，产水中尿素含量X＝(3.7-1.3)/0.2＝12ppb，极差为1，相对偏差8.3％，公式具有指导意义。
实施例3
将经过UF+RO处理后得到的再生水投加氧化剂后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有氧化剂的再生水进行照射，氧化剂包括如下质量分数的组分：6.0％双氧水、42.0％过二硫酸盐、2.0％氯胺和50.0％水。
再生水中尿素浓度为68ppb；
氧化剂的加入量为Y＝5.1ln(68)+2.9＝24.4ppm，取25ppm；
紫外氧化装置中水力停留时间为120s；
照射剂量为Z＝3.4(68) 0.8＝99.4mJ/cm 2，取100mJ/cm 2；
经检测，产水TOC浓度为9.7ppb。
将产水通入树脂柱，经检测，树脂柱出水的TOC浓度为2.9ppb，尿素浓度为8ppb；尿素去除率为88.24％。经换算，产水中尿素含量X＝(2.9-1.3)/0.2＝8ppb，极差为0，相对偏差0％，公式具有指导意义。
实施例4-调节了氧化剂的组成比例
将经过UF+RO处理后得到的再生水投加氧化剂后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有氧化剂的再生水进行照射，氧化剂包括如下质量分数的组分：7.0％双氧水、40.0％过二硫酸盐、3.0％氯胺和50.0％水。
再生水中尿素浓度为68ppb；
氧化剂的加入量为Y＝5.1ln(68)+2.9＝24.4ppm，取25ppm；
紫外氧化装置中水力停留时间为120s；
照射剂量为Z＝3.4(68) 0.8＝99.4mJ/cm 2，取100mJ/cm 2；
经检测，产水TOC浓度为10.1ppb。
将产水通入树脂柱，经检测，树脂柱出水的TOC浓度为3.0pb，尿素浓度为9ppb；尿素去除率为86.76％。经换算，产水中尿素含量X＝(3.0-1.3)/0.2＝8.5ppb，极差为0.5，相对偏差5.9％，公式具有指导意义。
对比实施例1-调整了氧化剂的加入浓度
将经过UF+RO处理后得到的再生水投加氧化剂后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有氧化剂的再生水进行照射，氧化剂包括如下质量分数的组分：6.0％双氧水、42.0％过二硫酸盐、2.0％氯胺和50.0％水。
再生水中尿素浓度为123ppb；
氧化剂的理论加入量为Y＝5.1ln(123)+2.9＝27.4ppm，实际加入量为20ppm；
紫外氧化装置中水力停留时间为120s；
照射剂量为Z＝3.4(123) 0.8＝159.7mJ/cm 2，取160mJ/cm 2；
经检测，产水TOC浓度为18.9ppb。
将产水通入树脂柱，经检测，树脂柱出水的TOC浓度为11.2pb，尿素浓度为48ppb；尿素去除率为60.98％，比实施例1减少17.07％。通过实施例1和对比实施例1可知，当氧化剂加入量不够，无法达到好的尿素去除效果。
对比实施例2-调整为单一氧化剂
将经过UF+RO处理后得到的再生水投加双氧水后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有双氧水的再生水进行照射。
再生水中尿素浓度为123ppb；
双氧水的加入量为30ppm(30ppm是指混合液中双氧水的浓度)；
紫外氧化装置中水力停留时间为120s；
照射剂量为160mJ/cm 2；
将产水通入树脂柱，经检测，树脂柱出水的尿素浓度为98ppb，尿素去除率为20.3％。对比实施例3-调整为单一氧化剂
将经过UF+RO处理后得到的再生水投加过二硫酸盐后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有过二硫酸盐的再生水进行照射。
再生水中尿素浓度为123ppb；
过二硫酸盐的加入量为30ppm；
紫外氧化装置中水力停留时间为120s；
照射剂量为160mJ/cm 2；
将产水通入树脂柱，经检测，树脂柱出水的尿素浓度为69ppb，尿素去除率为43.9％。对比实施例4-调整为单一氧化剂
将经过UF+RO处理后得到的再生水投加过一硫酸盐后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有过一硫酸盐的再生水进行照射。
再生水中尿素浓度为123ppb；
过一硫酸盐的加入量为30ppm；
紫外氧化装置中水力停留时间为120s；
照射剂量为160mJ/cm 2；
将产水通入树脂柱，经检测，树脂柱出水的尿素浓度为108ppb，尿素去除率为12.2％。
对比实施例5-调整为单一氧化剂
将经过UF+RO处理后得到的再生水投加氯胺后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有氯胺的再生水进行照射。
再生水中尿素浓度为123ppb；
氯胺的加入量为30ppm；
紫外氧化装置中水力停留时间为120s；
照射剂量为160mJ/cm 2；
将产水通入树脂柱，经检测，树脂柱出水的尿素浓度为110ppb，尿素去除率为10.6％。
对比实施例6-调整为两种氧化剂耦合
往经过UF+RO处理后得到的再生水中投加过双氧水和过二硫酸盐的混合液后通入紫外氧化装置，紫外氧化装置中安装有紫外灯管，通过紫外灯管对添加有混合液的再生水进行照射，混合液包括如下质量分数的组分：6.0％双氧水、42.0％过二硫酸盐和52.0％水。
再生水中尿素浓度为123ppb；
双氧水和二硫酸盐的总加入量为30ppm；
紫外氧化装置中水力停留时间为120s；
照射剂量为160mJ/cm 2；
将产水通入树脂柱，经检测，树脂柱出水的尿素浓度为37ppb，尿素去除率为69.9％。
通过实施例1和对比实施例2～6可知，针对再生水中痕量尿素的去除，单一氧化剂或两种氧化剂耦合均无法达到本发明氧化剂的去除效果，具体原因，一方面跟尿素本身的分子结构(氨基)有关，另一方面也与单一氧化剂自身以及产生的自由基的量和氧化能力有关，多个氧化剂能够彼此协同激发产生更多与尿素反应的自由基。本发明的氧化剂可以针对尿素本身分子结构产生具有强氧化能力的亲电子性自由基，从而实现再生水中尿素的高效去除。

Claims (7)

  1. 一种再生水中痕量小分子有机物的去除方法，其特征在于：将添加有氧化剂的反渗透再生水通入紫外氧化装置中，在紫外光照射下氧化剂与再生水中痕量小分子有机物发生氧化还原反应；反应时间为30～300s；其中，氧化剂包括如下质量分数的组分：6.0％～7.0％双氧水、40.0％～42.0％过二硫酸盐、2.0％～3.0％氯胺和48.0％～50.0％水；其中，反渗透再生水中尿素初始浓度为60ppb～125ppb，处理后产水中尿素浓度降低到5ppb。
  2. 根据权利要求1所述的再生水中痕量小分子有机物的去除方法，其特征在于：氧化剂中有效成分浓度与再生水中尿素浓度的关系式为：Y＝5.1ln(X)+2.9；
    式中，X为再生水中尿素浓度，单位ppb；Y为氧化剂中有效成分浓度，单位ppm。
  3. 根据权利要求1所述的再生水中痕量小分子有机物的去除方法，其特征在于：紫外光照射剂量与再生水中尿素浓度的关系式为：Z＝3.4X 0.8；
    式中，X为再生水中尿素浓度，单位ppb；Z为紫外光照射剂量，单位mJ/cm 2。
  4. 根据权利要求1所述的再生水中痕量小分子有机物的去除方法，其特征在于：所述再生水采用如下方法得到：将收集的污水厂尾水依次通过多介质过滤器、保安过滤器、超滤装置和反渗透装置，得到再生水。
  5. 根据权利要求1所述的再生水中痕量小分子有机物的去除方法，其特征在于：将氧化还原反应后的产水通入树脂柱中，通过检测树脂柱出水的TOC浓度，经换算得到氧化还原反应后产水中的尿素浓度。
  6. 根据权利要求5所述的树脂柱出水TOC换算尿素，其特征在于：树脂柱出水TOC浓度与氧化还原反应后产水中尿素浓度的关系式为：W＝0.2X+1.3；
    式中，X为氧化还原反应后产水中尿素浓度，单位ppb；W为树脂柱出水TOC浓度，单位ppb。
  7. 根据权利要求5所述的树脂柱出水TOC换算尿素，其特征在于：所述树脂柱内填充有强酸阳离子交换树脂和强碱阴离子交换树脂。
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