CN1256250A - Water purifying process including micro flocculation of inorganic high-molecular flocculant and direct deep-bed filtration - Google Patents

Abstract

Translated fromChinese

本发明涉及一种无机高分子絮凝剂(聚合铝、聚合铁)的微絮凝—深床直接过滤净水处理工艺,该工艺特征在于:它依据无机高分子絮凝剂强烈的吸附/电中和凝聚作用及其粘结架桥絮凝效能而设计微絮凝—深床直接过滤工艺系统。该工艺适用于低温、低浊、低色及富藻的城镇饮用水、工艺给水处理以及污水回用的深度处理,特别适用于水质浊度单位不大于20NTU,色度单位不大于20APHA(铂－钴比色单位)的水库、湖泊的中小水厂净水处理。与传统混凝—沉淀—澄清—过滤水处理工艺技术相比,该工艺省略了絮凝反应池与沉淀澄清池,因而具有流程短、过程简捷、自控程度高、占地面积小、可显著节省基建投资与运行絮凝药剂费、并提高单位产水率以及处理水质好等优点。The invention relates to a micro-flocculation-deep bed direct filtration water purification treatment process of inorganic polymer flocculants (polymeric aluminum, polymeric iron), the process is characterized in that it is based on the strong adsorption/electroneutralization and coagulation of inorganic polymer flocculants The micro-flocculation-deep bed direct filtration process system is designed based on the effect and its bonding and bridging flocculation efficiency. This process is suitable for the advanced treatment of low-temperature, low-turbidity, low-color and algae-rich urban drinking water, process water treatment and sewage reuse. It is especially suitable for water quality with a turbidity unit of no more than 20NTU and a chromaticity unit of no more than 20APHA (platinum- Cobalt colorimetric unit) water purification treatment of small and medium-sized water plants in reservoirs and lakes. Compared with the traditional coagulation-sedimentation-clarification-filtration water treatment process technology, this process omits the flocculation reaction tank and sedimentation clarification tank, so it has short process, simple process, high degree of self-control, small footprint, and can significantly save infrastructure. The cost of investment and operation of flocculation chemicals, and the increase of unit water production rate and good water quality and other advantages.

Description

Translated fromChinese

无机高分子絮凝剂的微絮凝—深床直接过滤净水处理工艺Micro-flocculation of inorganic polymer flocculant-deep bed direct filtration water purification process

本发明专利涉及一种适合于无机高分子絮凝剂高效絮凝反应特点的微絮凝一深床直接过滤工艺，该工艺适用于城镇饮用水、工业给水或废水回用深度处理领域，特别适用于以湖泊、水库的低温、地浊，富藻高色水质作为饮用源水的中小城镇净水处理。The patent of the invention relates to a micro-flocculation-deep bed direct filtration process suitable for the high-efficiency flocculation reaction characteristics of inorganic polymer flocculants. This process is suitable for the advanced treatment of urban drinking water, industrial water supply or wastewater reuse, especially for lakes. , The low temperature of the reservoir, the turbidity of the ground, the water quality of rich algae and high color are used as the water purification treatment of small and medium-sized towns as drinking source water.

随着当前社会经济的高速发展，人民生活水平与质量的提高，人民对饮用水质量问题倍加关注，各国饮用水水质标准也趋于更严格，更规范。因此，安全、卫生的饮用水净化处理已成为当今国内外水处理领域研究的重点及热门课题。With the rapid development of the current social economy and the improvement of people's living standards and quality, people pay more attention to the quality of drinking water, and the drinking water quality standards of various countries tend to be stricter and more standardized. Therefore, safe and hygienic drinking water purification treatment has become the focus and hot topic of research in the field of water treatment at home and abroad.

然而，由于当前工农业废水的大量排放，已导致河流水质污染问题日趋严重，饮用水源水质微污染状况日趋严重，尤其城镇中、小河流已成为当地工业废水及生活污水的纳污地。因此，水库、湖泊水质已成为当今世界范围内重要饮用水源地。然而，水库、湖泊的低温低浊、低色、富藻水质的净化处理又成为当前给水处理的重点及难点之一。However, due to the current large-scale discharge of industrial and agricultural wastewater, the problem of river water pollution has become increasingly serious, and the micro-pollution of drinking water source water has become increasingly serious. In particular, small and medium-sized rivers in cities and towns have become local industrial wastewater and domestic sewage. Therefore, the water quality of reservoirs and lakes has become an important source of drinking water in the world today. However, the low-temperature, low-turbidity, low-color, and algae-rich water purification treatment of reservoirs and lakes has become one of the key and difficult points of current water supply treatment.

传统给水净化处理工艺在处理这类水质时的主要问题在于，由于水中颗粒数目少、碰撞效率低而导致去除效果差。因此，需要在混凝处理工况，通过投加粘土颗粒或增加混凝剂剂量来增强颗粒碰撞几率，这不仅显著增加了药剂费用，同时也导致污泥量增加，继而增加了后续工艺负荷。同时，传统过滤工况的滤床较浅、滤料粒径小，从而导致了截污量小、运行周期短、产水率低等诸多问题。使用双层滤料或多层滤料可以提高截污量和滤速，但存在反冲洗困难，容易混层等缺点。此外，由于传统凝聚剂反应速度慢且对源水化学条件较敏感，絮凝净化效能低，这一切不仅造成现有水厂处理过程不畅，絮体上浮，滤池堵塞，处理费用显著增加，而且还导致水质超标，产水率下降等一系列问题。The main problem of the traditional feed water purification treatment process when dealing with this kind of water quality is that the removal effect is poor due to the small number of particles in the water and the low collision efficiency. Therefore, it is necessary to increase the probability of particle collision by adding clay particles or increasing the dose of coagulant in the coagulation treatment condition, which not only significantly increases the cost of the agent, but also leads to an increase in the amount of sludge, which in turn increases the subsequent process load. At the same time, the filter bed of the traditional filtration working condition is shallow and the particle size of the filter material is small, which leads to many problems such as small sewage interception, short operation cycle, and low water production rate. The use of double-layer filter materials or multi-layer filter materials can increase the interception capacity and filtration rate, but there are disadvantages such as difficult backwashing and easy mixing of layers. In addition, due to the slow reaction speed of traditional coagulants and their sensitivity to the chemical conditions of source water, the flocculation and purification efficiency is low. It also leads to a series of problems such as excessive water quality and decreased water production rate.

早在70年代，美国Wisner等人研究证明，直接过滤对此类水质净化处理效果较好，而且可省去了传统工艺中的絮凝反应与沉淀澄清步骤，明显节省基建投资；且在合适水力条件下，可显著节省药剂投加量，延长过滤周期，减少污泥负荷，因而可显著节省操作运行费用。目前直接过滤工艺在美国、法国、澳大利亚等发达国家已得到较多的应用，尽管目前国内外都在研究开发直接过滤工艺技术，也有许多文献报道，但国外直接过滤工艺均采用传统硫酸铝或氯化铁作为凝聚剂，同时还需辅助阳离子型高分子絮凝剂，并以非离子型高分子絮凝剂作为过滤助剂。工艺过程较为复杂，投药品种多而控制难，且存在有机高分子潜在毒性问题，因此不适合我国给水净化处理。国内曾报道直接过滤工艺，滤床填充滤料深度一般仅现于1.2-2.0m，所用滤料粒径均在1.2-1.8mm，滤速也仅为10-12m，因此其处理效果不甚显著。As early as the 1970s, research by Wisner et al. in the United States proved that direct filtration has a better effect on this type of water purification, and can save the flocculation reaction and sedimentation clarification steps in the traditional process, significantly saving infrastructure investment; and under suitable hydraulic conditions It can significantly save the dosage of chemicals, prolong the filtration cycle, reduce the sludge load, and thus significantly save operating costs. At present, the direct filtration process has been widely used in developed countries such as the United States, France, and Australia. Although the direct filtration process technology is being researched and developed at home and abroad, and there are many literature reports, the foreign direct filtration process uses traditional aluminum sulfate or chlorine. Ferric iron is used as a coagulant, and an auxiliary cationic polymer flocculant is also required, and a non-ionic polymer flocculant is used as a filter aid. The process is relatively complicated, there are many kinds of drugs and it is difficult to control, and there are potential toxicity problems of organic polymers, so it is not suitable for water purification in my country. The direct filtration process has been reported in China. The depth of the filter material filled in the filter bed is generally only 1.2-2.0m, the particle size of the filter material used is 1.2-1.8mm, and the filtration rate is only 10-12m, so the treatment effect is not very significant. .

本发明目的在于提供一种适合于无机高分子絮凝剂高效絮凝反应特点的微絮凝—深床直接过滤净水工艺，它适用于低温、低浊、低色，富藻及有机物微污染的水库或湖泊水质，以及工业给水深度处理，含油废水、城市污水回用深度处理。该工艺也可用于现有传统过滤工艺的技术改造。该工艺具有处理水质好，运行周期长，产水率大，运行稳定，并且可显著节省基建费和降低药剂运行费，适用自动控制等优点。The purpose of the present invention is to provide a micro-flocculation-deep bed direct filtration water purification process suitable for the high-efficiency flocculation reaction characteristics of inorganic polymer flocculants. Lake water quality, advanced treatment of industrial water supply, advanced treatment of oily wastewater and urban sewage reuse. This process can also be used in the technical transformation of the existing traditional filtration process. The process has the advantages of good water quality, long operation period, high water production rate, stable operation, and can significantly save infrastructure costs and chemical operating costs, and is suitable for automatic control.

本发明工艺流程是：被处理水与无机高分子絮凝剂通过在线管式混合器或机械搅拌槽短暂混合反应后(1-3分钟)，直接进入深床滤池进行净化处理。本发明主要特点在于：The technological process of the present invention is: the treated water and the inorganic macromolecule flocculant are mixed and reacted briefly (1-3 minutes) by an online tubular mixer or a mechanical stirring tank, and then directly enter a deep bed filter tank for purification treatment. Main features of the present invention are:

1.它依据无机高分子絮凝剂(聚合氯化铝，聚合氯化铁，聚合硅铝)中的多羟基聚合络离子与水中胶体颗粒的强烈吸附/电中和凝聚脱稳，投加水中后即可迅速发生吸附凝聚脱稳而快速形成微絮体颗粒的特点，依据源水水质条件而通过计量泵与流动电流严格控制无机高分子絮凝剂的投加剂量，保证原水中杂质颗粒与絮凝剂发生强烈的电中和/吸附凝聚脱稳最佳投加剂量。1. It is based on the strong adsorption/electroneutralization and coagulation destabilization of polyhydroxy polymeric complex ions in inorganic polymer flocculants (polyaluminum chloride, polyferric chloride, polysilicon aluminum) and colloidal particles in water. The characteristics of rapid adsorption, coagulation and destabilization and the rapid formation of micro-flocculent particles, according to the water quality conditions of the source water, the dosage of the inorganic polymer flocculant is strictly controlled through the metering pump and the flowing current to ensure that the impurity particles in the raw water and the flocculant The best dosage for strong charge neutralization/adsorption coagulation destabilization.

2.采用管式在线混合器，管式混合的水力条件控制为1-3分钟，保证投药后的原水进入滤池前只产生微絮凝矾花(粒径范围在50-100μm弱正电性的微絮体颗粒)，矾花增长和沉降过程在滤层中完成。因此滤池的截污分布均匀，有效深度大，同时省去传统工艺中的混合池和反应池，节省基建投资。2. Using a tubular online mixer, the hydraulic condition of the tubular mixing is controlled for 1-3 minutes to ensure that the raw water after dosing only produces micro-flocculated alum flowers (with a particle size range of 50-100 μm and weak positive charge) before entering the filter. Microfloc particles), the growth and sedimentation process of alum flowers are completed in the filter layer. Therefore, the sewage interception distribution of the filter is uniform, and the effective depth is large. At the same time, the mixing tank and reaction tank in the traditional process are omitted, which saves infrastructure investment.

3.根据吸附在水中胶体颗粒表面上的无机高分子絮凝剂具有强烈的粘附架桥的絮凝特点以及由于水动力紊流运动在超大滤料间形成的微涡旋作用，采用均质超大滤料。滤料平均粒径在2.0-4.0mm，不均匀系数为1.2～1.5。滤床深度在3-5米，滤料填充高度为1.5-3米。保证增加微矾花絮体颗粒间的碰撞几率以及粘附架桥能力而被有效拦截在滤料间隙中，从而保证料在出水水质优良条件下，滤池截污能力明显提高，运行周期和产水率显著增加，而絮凝剂投加量则显著减少。3. According to the strong adhesion and bridging flocculation characteristics of the inorganic polymer flocculant adsorbed on the surface of the colloidal particles in the water and the micro-vortex effect formed between the ultra-large filter materials due to the hydrodynamic turbulent movement, the homogeneous ultra-large filter material. The average particle size of the filter material is 2.0-4.0mm, and the non-uniformity coefficient is 1.2-1.5. The depth of the filter bed is 3-5 meters, and the filling height of the filter material is 1.5-3 meters. Ensure that the collision probability between the micro-alum floc particles and the adhesion and bridging ability are effectively intercepted in the gap of the filter material, so as to ensure that the filter's sewage interception ability is significantly improved under the condition of good effluent water quality, and the operation cycle and water production The rate increased significantly, while the flocculant dosage decreased significantly.

本发明工艺技术试验流程系统如附图1所示，装置具体尺寸参数如下：滤柱高500cm，内径20cm，承托层20cm。无烟煤粒径范围为2.0-2.5mm和3.5-4.0mm，不均匀系数1.05-1.1。滤层填充高度为1米-2.5米。进水直接与水厂配水管路相连，承托层铺垫颗粒粒径16-32mm、8～16mm、4-8mm的卵石。设计处理量为1吨/小时，滤速为30米。The process technology test flow system of the present invention is shown in Figure 1, and the specific size parameters of the device are as follows: the filter column is 500 cm high, the inner diameter is 20 cm, and the supporting layer is 20 cm. The particle size range of anthracite is 2.0-2.5mm and 3.5-4.0mm, and the non-uniformity coefficient is 1.05-1.1. The filling height of the filter layer is 1m-2.5m. The water inlet is directly connected to the water distribution pipeline of the water plant, and the supporting layer is paved with pebbles with a particle size of 16-32mm, 8-16mm, and 4-8mm. The design processing capacity is 1 ton/hour, and the filtration speed is 30 meters.

流程：源水由源水储槽经泵进入管式混合器，在管式混合器前由高精度电子蠕动计量泵控制加注絮凝剂剂量，经原水与絮凝剂经管式混合器混合1分钟后直接进入滤柱进行截污处理。出水浊度采在线浊度监测仪进行在线检测并记录。滤速控制在16～31m/h，水头损失穿透标准设定为220cm，水质穿透标准设定为浊度＜0.3NTU，色度＜0.5APHA，与国外水质标准一致。Process: The source water enters the tubular mixer from the source water storage tank through the pump, and the high-precision electronic peristaltic metering pump controls the amount of flocculant before the tubular mixer, and the raw water and the flocculant are mixed by the tubular mixer for 1 minute. Directly enter the filter column for sewage interception treatment. The turbidity of the effluent is detected and recorded online with an online turbidity monitor. The filtration rate is controlled at 16-31m/h, the water head loss penetration standard is set at 220cm, and the water quality penetration standard is set at turbidity<0.3NTU and chroma<0.5APHA, which are consistent with foreign water quality standards.

下面通过实用实施例具体来说明本发明工艺净水处理之优点：应用实施例1：The advantage of process water purification treatment of the present invention is specifically described below by practical embodiment: application example 1:

原水浊度8.2～9.7NTU，色度为0～7.5APHA(铂钴比色法色度单位)，水温0～10℃，pH为6.8～7.1。采用无烟煤滤料，滤料粒径2.0～2.2mm，不均匀系数1.2，填料深度为2米。管式混合，停留时间2分钟，GT值为1200。初始滤速为20m/hr。最终滤速为18m/hr。絮凝剂采用聚合氯化铝(碱化度50～60％)和硫酸铝，投加量为0.75～1.0mg/L(以Al₂O₃计，下同)。净水处理对比效果见表1。应用实施例2：The turbidity of raw water is 8.2-9.7NTU, the chromaticity is 0-7.5APHA (platinum-cobalt colorimetric colorimetric unit), the water temperature is 0-10°C, and the pH is 6.8-7.1. Anthracite filter material is used, the particle size of the filter material is 2.0-2.2mm, the coefficient of non-uniformity is 1.2, and the filling depth is 2 meters. Tube mixing, residence time 2 minutes, GT value 1200. The initial filtration rate is 20m/hr. The final filtration rate is 18m/hr. The flocculants are polyaluminum chloride (alkalinity: 50-60%) and aluminum sulfate, and the dosage is 0.75-1.0 mg/L (calculated as Al₂ O₃ , the same below). The comparison effect of water purification treatment is shown in Table 1. Application Example 2:

原水浊度分别为7.5～8.5NTU，色度为30～50APHA(铂钴比色法色度单位)，水温为10～15℃，pH为7.2～7.5。采用石英砂滤料，粒径1.7～1.9mm，不均匀系数1.18，填充滤料深度为2米。管式加机械搅拌混合，停留时间2分钟，GT值为1400。初始滤速为2m/hr。最终滤速为18m/hr。絮凝剂为聚合氯化铁(碱化度15～24％)和三氯化铁，在相同投加量为3～6mg/L(以Al₂O₃计，下同)条件下。净水处理效果对比见表2。Raw water turbidity is 7.5-8.5NTU, chromaticity is 30-50 APHA (platinum-cobalt colorimetric colorimetric unit), water temperature is 10-15°C, and pH is 7.2-7.5. Quartz sand filter material is used, the particle size is 1.7-1.9mm, the non-uniformity coefficient is 1.18, and the filling depth of the filter material is 2 meters. Tubular mixing with mechanical stirring, residence time 2 minutes, GT value 1400. The initial filtration rate is 2m/hr. The final filtration rate is 18m/hr. The flocculant is polyferric chloride (alkalinization degree: 15-24%) and ferric trichloride, under the same dosage of 3-6 mg/L (calculated as Al₂ O₃ , the same below). The comparison of water purification treatment effect is shown in Table 2.

             表1、聚合铝絮凝剂与三氯化铝/硫酸铝凝聚剂          Table 1, Polyaluminum flocculants and aluminum trichloride/aluminum sulfate coagulants

             在微絮凝—深床直接过滤工艺中净水效果的对比   絮凝剂    投药剂量( mg/l)    浊度(NTU)进水   出水    色度(APHA)进水     出水   水温℃     水头损失(cm/hr)   过滤周期(hr)    周期产水率(m³/m²) PAC-50    0.75  8.9    0.02 0.0      0.0    10     0.091    26     468 AlCl₃    0.75  8.9    0.27 0.0      0.0    10     0.107     8     145 PAC-60    0.75  8.2    0.08 0.0      0.0     5     0.087    25     452 AlCl₃    1.25  8.2    0.32 0.0      0.0     5     0.097    14     252 PAC-60    1.35  9.8    0.20 7.4      0.2     3     0.115    15     277 AlCl₃    1.35  9.8    1.2 7.4      2.7     3     0.191     7     126 PAC-60    1.0  8.7    0.5 7.2      0.1     5     0.106    16     293 AlSO₄    2.55  8.7    0.5 7.2      0.5     5     0.153     5     75Comparison of water purification effect in micro-flocculation-deep bed direct filtration process flocculant Dosage (mg/l) Turbidity (NTU) Inlet Water Outlet Chromaticity (APHA) Inlet Water Outlet Water temperature ℃ Head loss (cm/hr) Filtration cycle (hr) Periodic water production rate (m³ /m² ) PAC-50 0.75 8.9 0.02 0.0 0.0 10 0.091 26 468_AlCl3 0.75 8.9 0.27 0.0 0.0 10 0.107 8 145 PAC-60 0.75 8.2 0.08 0.0 0.0 5 0.087 25 452_AlCl3 1.25 8.2 0.32 0.0 0.0 5 0.097 14 252 PAC-60 1.35 9.8 0.20 7.4 0.2 3 0.115 15 277_AlCl3 1.35 9.8 1.2 7.4 2.7 3 0.191 7 126 PAC-60 1.0 8.7 0.5 7.2 0.1 5 0.106 16 293 AlSO₄ 2.55 8.7 0.5 7.2 0.5 5 0.153 5 75

         表2、聚合氯化铁絮凝剂与三氯化铁凝聚剂     Table 2. Polymerized ferric chloride flocculant and ferric chloride flocculant

       在微絮凝—深床直接过滤工艺中净水效果的对比   水头损失(m/hr)     出水水质(NTU)   出水水质(色度)  运行周期(hr)     产水率(m³/m²) 1)原水水质    7.5-8.5NTU     30-35 PFC-A     0.15       0.05      ＜3      19.5      270 PFC-B     0.14       0.03      ＜3       20      280 FeCl₃     0.26       0.03      ＜3      11.5      160 2)原水水质     50-60NTU      50 PFC-A     0.21       0.12      ＜5      14.5      200 PFC-B     0.23       0.10      ＜5      13.5      190 FeCl₃     0.32       0.05      ＜5      7.5      105Comparison of water purification effect in micro-flocculation-deep bed direct filtration process Head loss (m/hr) Effluent water quality (NTU) Water quality (color) Operating cycle (hr) Water production rate (m³ /m² ) 1) Raw water quality 7.5-8.5NTU 30-35 PFC-A 0.15 0.05 <3 19.5 270 PFC-B 0.14 0.03 <3 20 280_FeCl3 0.26 0.03 <3 11.5 160 2) Raw water quality 50-60NTU 50 PFC-A 0.21 0.12 <5 14.5 200 PFC-B 0.23 0.10 <5 13.5 190_FeCl3 0.32 0.05 <5 7.5 105

表1和表2的应用实例结果可见，在不同水质，相同或低于传统凝聚剂投加剂量条件下，无机高分子絮凝剂无论在运行周期，出水水质以及产水率方面均明显高于传统凝聚剂，表明本发明所述微絮凝—深床直接净水处理工艺完全适合于无机高分子絮凝剂的高效絮凝反应特点，具有显著的除浊除色净水效能。应用实施例3The results of the application examples in Table 1 and Table 2 show that under the condition of different water quality and the same or lower dosage of traditional coagulant, the inorganic polymer flocculant is significantly higher than the traditional coagulant in terms of operation cycle, effluent water quality and water production rate. The coagulant shows that the micro-flocculation-deep bed direct water purification treatment process described in the present invention is completely suitable for the high-efficiency flocculation reaction characteristics of the inorganic polymer flocculant, and has remarkable turbidity, color and water purification performance. Application Example 3

为了更清楚地说明本发明工艺的实际净水处理之优点，本发明工艺系统在北京水源九厂导示试验厂进行长期(10个月)低浊水(1.8-3.0NTU)实际净水处理运行试验，并同时与该厂目前运行工艺系统进行了对比。。根据该水厂的常年水质浊度平均低于5NTU的情况，水厂实际运行试验进一步调整，采用超大无烟煤滤料，粒径3.5～4.0mm，当直径de＝3.8mm，不均匀系数1.05。滤层厚度为2～2.5m.。混合采用管式混合与机械搅拌混合，GT值1200～1500。典型运行试验对比结果分别见表3和表4。In order to illustrate the advantages of the actual water purification treatment of the process of the present invention more clearly, the process system of the present invention was carried out in the Beijing Water Source No. 9 Plant Guidance Test Plant for long-term (10 months) low turbidity water (1.8-3.0NTU) actual water purification treatment operation At the same time, it was compared with the current operating process system of the plant. . According to the fact that the average annual water turbidity of the water plant is lower than 5NTU, the actual operation test of the water plant was further adjusted, using super large anthracite filter material with a particle size of 3.5-4.0mm, when the diameter de=3.8mm, and the non-uniformity coefficient of 1.05. The thickness of the filter layer is 2-2.5m. The mixing adopts tubular mixing and mechanical stirring, and the GT value is 1200-1500. The comparative results of typical running tests are shown in Table 3 and Table 4 respectively.

                表3、北京水厂实际运行净水处理结果 编号        浊度(NTU)    滤床床深(m)    投药剂量(mg/l)   水头增长速率(cm/hr)   过滤周期(hr)   过滤滤速(m/h)   周期产水率(m³/m²)   反冲洗用水率(％)    进水    出水   1    1.50    0.20      2     0.4    5.62     25     32     775    0.86   2    1.83    0.21      2     0.48    4.47     34     25     867    1.09   3    1.76    0.2     2.5     0.4    4.57     96     16    1536    1.01   4    1.87    0.21     2.5     0.32    2.12     95     16    1520    1.12   5    2.53    0.15     2.5     0.48    5.67     74     16    1184    1.12   6    2.47    0.2     2.5     0.68    6.32     78     16    1242    1.05   7    2.52    0.6     2.5     0.4    7.35     68     24    1632    0.97   8    2.34    0.48     2.5     0.48    6.54     62     24    1440    1.07   9    1.67    0.13     2.5     0.48    7.14     28     31     868    0.89   10    1.38    0.18     2.5     0.4    3.24     71     24    1420    1.03表4、微絮凝—深床直接过滤工艺与水厂现有处理工艺的实际运行结果对比工艺流程   过滤滤速(m/hr)       投药剂量范围(mg/L Al₂O₃)       周期产水率(m³/m²)     反冲洗用水率(％) 水厂运行工艺系统 混合池三级絮凝反应池斜板沉淀池无烟煤滤池碳滤池出水    7～8      0.6～0.8     336～384    1.5～1.6 本发明的工艺系统 混合池深床过滤碳滤池出水   16～32     0.32～0.48    1200～1500    0.8～1.1Table 3. Results of water purification treatment in actual operation of Beijing Water Plant serial number Turbidity (NTU) Depth of filter bed (m) Dosage (mg/l) Head growth rate (cm/hr) Filtration cycle (hr) Filtration speed(m/h) Periodic water production rate (m³ /m² ) Backwash water rate (%) flooded out of water 1 1.50 0.20 2 0.4 5.62 25 32 775 0.86 2 1.83 0.21 2 0.48 4.47 34 25 867 1.09 3 1.76 0.2 2.5 0.4 4.57 96 16 1536 1.01 4 1.87 0.21 2.5 0.32 2.12 95 16 1520 1.12 5 2.53 0.15 2.5 0.48 5.67 74 16 1184 1.12 6 2.47 0.2 2.5 0.68 6.32 78 16 1242 1.05 7 2.52 0.6 2.5 0.4 7.35 68 twenty four 1632 0.97 8 2.34 0.48 2.5 0.48 6.54 62 twenty four 1440 1.07 9 1.67 0.13 2.5 0.48 7.14 28 31 868 0.89 10 1.38 0.18 2.5 0.4 3.24 71 twenty four 1420 1.03 Table 4. Comparison of the actual operation results of the micro-flocculation-deep bed direct filtration process and the existing treatment process of the water plant process flow Filtration rate(m/hr) Dosage range (mg/L Al₂ O₃ ) Periodic water production rate (m³ /m² ) Backwash water rate (%) Water plant operation process system Mixing tankThree-stage flocculation reaction tankIncline plate sedimentation tankAnthracite filterCarbon filterWater 7～8 0.6～0.8 336～384 1.5～1.6 Process system of the present invention Mixing pool, deep bed filtration, carbon filter, effluent 16～32 0.32～0.48 1200～1500 0.8～1.1

从表4对比结果可见，本发明净水工艺具有如下几方面优点：1)在工艺流程方面，本发明工艺流程省略了絮凝反应及沉淀过程，因此仅在工艺流程方面可直接节省工艺投资费近1/3。2)在产水率方面，现有水厂过滤池采用浅床结构，滤速为7-8m/hr，48小时进行反冲洗，而按目前本发明的微絮凝—深床直接过滤工艺滤速控制16m/hr，稳定运行高达80-96小时，滤速比现有传统工艺提高1倍，过滤周期也提高1倍，由此日产水率提高近4倍。仅此，水厂每年所得社会与经济效益是十分可观的。3)在药剂方面：目前使用B值60％的液体聚合铝絮凝剂，在床深为2.5m，滤速16m/h时，投药量仅为2mg/L(商业重量)，只是现有水厂处理工艺投药量的1/3-1/2，稳定运行达到80-96小时。按目前日处理水量100万吨的水厂计算药耗量计算，现每天用药量为4吨，按每吨液体PAC市售1600元计算，每天仅药剂费就可节省3200元，每年则可达116.8万元。4)出水水质方面：试验水质控制标准为0.3NTU，明显地提高水厂出水水质(现有水厂出水水质标准为＜1NTU)，使出水水质达到发达国家水厂处理标准。这对提高我国水厂安全饮用水质量，保障人民身体健康无疑具有重要的社会意义和显著的经济效益。As can be seen from the comparative results of Table 4, the water purification process of the present invention has the advantages in the following aspects: 1) in the technical process, the technical process of the present invention omits the flocculation reaction and the sedimentation process, so only in the technical process, the process investment cost can be directly saved by nearly 1/3. 2) In terms of water production rate, the existing water plant filter tank adopts a shallow bed structure, and the filtration rate is 7-8m/hr, and backwashing is carried out in 48 hours, while the microflocculation-deep bed of the present invention directly The filtration rate of the filtration process is controlled at 16m/hr, and the stable operation is as high as 80-96 hours. The filtration rate is doubled compared with the existing traditional process, and the filtration cycle is also doubled, thereby increasing the daily water production rate by nearly 4 times. Only this, the social and economic benefits of the water plant every year are very considerable. 3) In terms of medicaments: currently using a liquid polymeric aluminum flocculant with a B value of 60%, when the bed depth is 2.5m and the filtration rate is 16m/h, the dosage is only 2mg/L (commercial weight). 1/3-1/2 of the dosage of the treatment process, and the stable operation reaches 80-96 hours. Calculated according to the chemical consumption calculated by the water plant with a daily water treatment capacity of 1 million tons, the current daily drug consumption is 4 tons, and based on the market price of 1,600 yuan per ton of liquid PAC, the daily drug fee alone can save 3,200 yuan, and the annual amount can reach 1.168 million yuan. 4) In terms of effluent water quality: the test water quality control standard is 0.3NTU, which significantly improves the effluent water quality of the water plant (the existing water plant effluent water quality standard is <1NTU), making the effluent water quality meet the treatment standards of water plants in developed countries. This undoubtedly has important social significance and significant economic benefits for improving the quality of safe drinking water in my country's water plants and ensuring people's health.

Claims (7)

Translated fromChinese

1.本发明涉及一种适合于无机高分子絮凝剂(聚合铝、聚合铁、聚铝硅)高效絮凝反应特点的微絮凝—深床直接过滤处理工艺，该工艺适用于低温、低浊、低色及富藻的城镇饮用水、工业给水处理以及污水回用深度处理，特别适用于水质浊度单位不大于20NTU，色度单位不大于20 APHA(铂-钴比色法单位)的水库、湖泊水的中小城镇净水处理。1. The present invention relates to a micro-flocculation-deep bed direct filtration treatment process suitable for the high-efficiency flocculation reaction characteristics of inorganic polymer flocculants (polymeric aluminum, polyferric, polyaluminum silicon), which is suitable for low temperature, low turbidity, low Color and algae-rich urban drinking water, industrial water supply treatment and advanced treatment of sewage reuse, especially suitable for reservoirs and lakes where the water quality turbidity unit is not greater than 20NTU, and the chromaticity unit is not greater than 20 APHA (platinum-cobalt colorimetry units) Water purification treatment for small and medium towns.2.根据权利1的要求，该工艺不仅适用于新建的微絮凝—深床直接过滤净水处理，还适用于现有传统过滤工艺的改造，它可显著提高出水水质、增加产水率、降低药耗。2. According to the requirements of claim 1, this process is not only suitable for newly-built micro-flocculation-deep bed direct filtration water purification treatment, but also suitable for the transformation of existing traditional filtration processes, which can significantly improve the quality of effluent water, increase water production rate, reduce Drug consumption.3.根据权利1的要求，其特征是过滤滤床深及滤料填充高度超过普通滤床一至二倍，滤床深度为3～5米，滤料填充高度为1.5～3米。3. According to the requirements of claim 1, it is characterized in that the depth of the filter bed and the filling height of the filter material are one to two times higher than that of the ordinary filter bed, the depth of the filter bed is 3 to 5 meters, and the filling height of the filter material is 1.5 to 3 meters.4.根据权利3的要求，其特征是滤床填充滤料为大粒径的均质无烟煤、石英砂或陶粒。滤料粒径范围为2.0-4.0毫米，不均匀系数一般要求1.2～1.4。4. According to the requirement of claim 3, it is characterized in that the filter material filled in the filter bed is homogeneous anthracite coal, quartz sand or ceramsite with large particle size. The particle size range of the filter material is 2.0-4.0 mm, and the non-uniformity coefficient generally requires 1.2-1.4.5根据权利1至4的要求，其特征是该工艺技术的过滤滤速为12～32米。5. According to the requirements of claims 1 to 4, it is characterized in that the filtration rate of the process technology is 12 to 32 meters.6.根据权利1至5的要求，其特征是微絮凝—深床直接过滤过程使用无机高分子絮凝剂(包括聚合氯化铝、聚合氯化铁、聚合硫酸铁等)。6. According to the requirements of rights 1 to 5, it is characterized in that the micro-flocculation-deep bed direct filtration process uses an inorganic polymer flocculant (comprising polyaluminum chloride, polyferric chloride, polyferric sulfate, etc.).7.根据权利6的要求，其特征是无机高分子絮凝剂通过计量泵严格控制投加剂量，并与原水通过管式在线混合器或机械搅拌混合槽混合投加，混合停留时间控制在1-3分钟，混合后直接进入过滤滤床，无需再建造絮凝反应池和沉淀澄清池。7. According to the requirements of claim 6, it is characterized in that the dosage of the inorganic polymer flocculant is strictly controlled through the metering pump, and mixed with the raw water through a tubular online mixer or a mechanical stirring mixing tank, and the mixing residence time is controlled at 1- After 3 minutes, it will directly enter the filter bed after mixing, and there is no need to build a flocculation reaction tank and a sedimentation clarifier.

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