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УДК 66.081.63 DOI: 10.22227/1997-0935.2018.8.992-1007
Technical and economic comparison of the efficiency of drinking water preparation from underground water sources using the membrane technology of nanofiltration and traditional technologies
Yu Dan Su1, Alexey G. Pervov2, Vladimir A. Golovesov2
1RAIFIL China, CSM official representative in Russia, RM 206. Chengwen Business Building, No. 4285 Shendu Road, Shanghai, China; 2 Moscow State University of Civil Engineering (National Research University) (MGSU), 26 Yaroslavskoe shosse, Moscow, 129337, Russian Federation
ABSTRACT: Research subject: research on the improvement of modern membrane methods of well water purification with the purpose of creating a universal effective technology for removing hardness salts, iron, fluorides, ammonium, strontium from water, etc. from water. Experimental studies have been carried out to determine the quality of water purification by water membranes from iron ions, stiffness and fluoride, and also to determine the rates of formation of calcium carbonate precipitations on membranes. For various cases of well water cleaning in the Podolsky District of New Moscow, an economic comparison of the newly developed membrane technology with the "classical" technological solutions offered by the main leading domestic companies was carried out.
Objectives: justification of the effectiveness of the application of a newly developed membrane technology for the purification of well water based on a comparison of its economic and environmental indicators with the indicators of technologies currently existing in the market of water treatment equipment.
Materials and methods: an overview of the methods for cleaning well water from various contaminants, a description of technological schemes, and their advantages and disadvantages is shown. A new approach to the development of technological schemes for wastewater treatment with a minimum consumption of water for own needs is described, consisting in processing water in two stages. Experiments were carried out to determine the technological characteristics of membrane units (the filtrate output, the rates of precipitation formation on the membranes). The studies were carried out on laboratory stands using nanofiltration membranes with different selectivities indicators. The determination of the costs of service reagents and equipment costs was carried out with the help of calculations according to a program previously developed by
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filtrate output (0.75...0.9). In the development of units, preference should be given to the use of membranes with low selectivity, low energy consumption, and low reagent costs. This was demonstrated using the experimentally obtained dependences of the rate of growth of the calcium carbonate precipitate on the type of membranes and the multiplicity of the volumetric c concentration of the source water.
<D Conclusions: the use of universal membrane systems in container design for the purification of well water at a flow rate of
10 m3/h and above shows that even in the simplest cases (removal of only iron from water) the proposed technology demonstrates high economic and ecological effect in comparison with the technologies traditionally used for this purpose due to its simplicity, small size, the absence of reagents and wastewater. The use of universal units makes it possible to easily cover large areas with a large number of wells and consumers due to their construction, installation and maintenance according
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KEY WORDS: well water, iron and manganese removal, water softening, fluoride removal, reverse osmosis, nanofiltration, reduction of concentrate consumption
FOR CITATION: Yu Dan Su, Alexey G. Pervov, Vladimir A. Golovesov. Technical and economic comparison of the efficiency of preparation of drinking water from underground water sources with the use of membrane technology of nanofiltration and traditional technologies. Vestnik MGSU [Proceedings of Moscow State University of Civil Engineering]. 2018, vol. 13, issue 8 (119), pp. 992-1007. DOI: 10.22227/1997-0935.2018.8.992-1007
Технико-экономическое сравнение эффективности подготовки питьевой воды из подземных водоисточников с применением мембранной технологии нанофильтрации и традиционных технологий
Ю Дан Су1, А.Г. Первов2, В.А. Головесов2
'«RAIFIL China», представитель компании CSM в России, 201112, Китай, Шанхай, р-н Мин Ханг, Шен Ду Роуд, 4285, Ченг Вен Бизнес Билдинг, оф. 206; 2Национальный исследовательский Московский государственный строительный университет (НИУМГСУ), 129997, г. Москва, Ярославское шоссе, д. 26
Ф ¡2 АННОТАЦИЯ: Предмет исследования: исследования по совершенствованию современных мембранных методов
И ¡> очистки подземных вод с целью создания универсальной эффективной технологии удаления из воды солей жест-
992
© Yu Dan Su, Alexey G. Pervov, Vladimir A. Golovesov, 2018
кости, железа, фторидов, аммония, стронция и т.д. Проведены экспериментальные исследования, позволяющие определить качество очистки мембранами воды от ионов железа, жесткости и фтора, а также определить скорости образования отложений карбоната кальция на мембранах. Для различных случаев очистки подземных вод Подольского района Новой Москвы проведено экономическое сравнение разработанной новой мембранной технологии с «классическими» технологическими решениями, предлагаемыми основными ведущими отечественными компаниями. Цели: обоснование эффективности применения новой разработанной мембранной технологии для очистки подземных вод на основе сравнения ее экономических и экологических показателей с показателями технологий, существующих в настоящее время на рынке водоочистного оборудования.
Материалы и методы: представлен обзор методов очистки подземных вод от различных загрязнений, дано описание технологических схем, представлены их достоинства и недостатки. Описан новый подход к созданию технологических схем очистки сточных вод с минимальным расходом воды на собственные нужды, состоящий в обработке воды в две ступени. Проведены эксперименты по определению технологических характеристик мембранных установок (величин выхода фильтрата, интенсивностей образования осадков на мембранах). Исследования проводились на лабораторных стендах с использованием нанофильтрационных мембран с различными значениями селективностей. Определение расходов сервисных реагентов и затрат на оборудование проводились с помощью расчетов по программе, ранее разработанной авторами для определения технологических характеристик мембранных установок. Результаты: расчеты показывают, что мембраны эффективно задерживают ионы железа, жесткости и фтора даже при высоких значениях величины выхода фильтрата (0,75...0,9). При разработке установок предпочтение следует отдавать применению мембран с низкой селективностью, низким энергопотреблением и затратам на реагенты. Это продемонстрировано с помощью экспериментально полученных зависимостей скоростей роста осадка карбоната кальция от типа мембран и кратности объемного концентрирования исходной воды.
Выводы: применение универсальных мембранных систем в контейнерном исполнении при очистке подземных вод с расходом 10 м3/ч и выше показывает, что даже в самых простых случаях (удаление из воды только железа) предложенная технология демонстрирует высокие значения экономического и экологического эффекта по сравнению с традиционно используемыми для этих целей технологиями за счет простоты, компактности, отсутствия реагентов и сточных вод. Применение универсальных установок позволяет легко охватывать значительные территории с большим количеством скважин и потребителей благодаря их строительству, монтажу и обслуживанию по единой схеме.
КЛЮЧЕВЫЕ СЛОВА: подземные воды, удаление из воды железа и марганца, умягчение воды, удаление из воды фторидов, обратный осмос, нанофильтрация, сокращение расхода концентрата
ДЛЯ ЦИТИРОВАНИЯ: Ю Дан Су, Первов А.Г., Головесов В.А. Technical and economic comparison of the efficiency of drinking water preparation from underground water sources using the membrane technology of nanofiltration and traditional technologies // Вестник МГСУ. 2018. Т. 13. Вып. 8 (119). С. 992-1007. DOI: 10.22227/1997-0935.2018.8.992-1007
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INTRODUCTION
The purification of well water for drinking water supply in small towns, enterprises and individual houses is often a rather serious task. This is due to a change in the chemical composition of well water even within a small area and the difficulty in selecting technologies to remove various dissolved contaminants from them. A small change in the composition of well water (the increased content of fluoride, strontium in the well water, etc.) leads to the need for selection of a new purification technology. Thus, the solution of the problem of drinking water supply facilities in a relatively small area of New Moscow requires the development of water purification systems of various categories:
• waters with high iron content;
• waters with high iron content and hardness;
• water with a high content of not only iron and hardness, but also fluorides, as well as ammonium, strontium and other contaminants.
REVIEW OF LITERATURE
At present, a method of simplified aeration with subsequent filtration is used to remove iron from well water in small objects (Fig. 1, a). In cases where it is
necessary to remove not only iron but also hardness ions from the water, schemes are applied that include not only de-ironing equipment, but also The ones for water softening (mainly based on the sodium zeolite softening method), as shown in Fig. 1, b. If not only iron and salts of hardness, but also dissolved contaminants in the ionic form (fluorides, ammonium, strontium, arsenic, etc.) should be removed from the well water, then membrane units of nanofiltration or reverse osmosis are used (Fig. 1, c).
For the purification of well water, various types of equipment are often used [1]. Schemes of application of these types of equipment are constantly being improved. Thus, Fig. 2 shows different types of filters for removing iron from the water, using catalytic charges (Birm, Greensand, etc.) and various ways of oxidation of the source water.
For water supply of small objects, filters for de-ironing and softening (Fig. 2) are used in fiberglass plastic with special automatic valves and timers for flushing and regeneration [1]. The use of reverse osmosis installations is also based on various principles. The main difficulty in using membrane reverse osmosis installations is the need to pre-clean the source water and carry out special measures to remove the substances forming suspended solids and low-soluble
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Fig. 1. Technological schemes for the purification of natural waters: deferrization of water by the simplified aeration method with single-stage a and two-stage b filtration; c — deferrization by the simplified aeration method with nanofiltration; 1 — supply of source water; 2, 3 — fast light filter; 4 — disinfection of water; 5 — fluorination of water; 6 — aeration column; 7 — air blower (compressor); 8 — the raising pump; 9 — water tower
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Fig. 2. Technological scheme of well water treatment with the use of automated filters with catalytic loading and sodium zeolite softening process filters: 1 — filters with loading Birm or Greensand; 2 — automatic filter control unit; 3 — the compressor; 4 — a doser of calcium permanganate; 5 — consumption tank solution of potassium permanganate; 6 — filter with cation; 7 — tank — salt solvents of tableted salt; 8 — source water; 9 — purified water; 10 — water meter; 11 — discharge into sewerage; 12 — the air valve; 13 — check valve
salts (calcium carbonate) on the membranes from the source water [1-5]. Fig. 3 shows the scheme of well water treatment using the reverse osmosis system, in which iron removal system with simplified aeration was used as iron pre-treatment, and calcium carbonate precipitations were dosed into the water of the inhibitor Aminat K. The use of various inhibitory substances to prevent the formation of carbonate prepositions on the membranes constitutes an essential part of current research on the use of membrane methods in drinking water supply [6-8].
In some cases, filters for de-ironing and sodium zeolite softening process are used to pre-clean the water before reverse osmosis installations (Fig. 1, b). However, the application of such a pre-treatment scheme leads to an increase in operating costs and the formation of regeneration solutions with a high salt content. Among methods of removing iron from the water, used both as a pre-treatment before the reverse osmosis installations, and independently, sometimes ultrafiltration systems are used [6-10]. The technological schemes shown above possess a number of individual features and shortcomings. Thus, the method of simplified aeration may prove ineffective with a change in the oxidation-reduction potential of water. Water softening with the use of sodium zeolite softening process leads, as already mentioned above, to the extremely high costs of reagents (salt) and the formation of mineralized regenerative effluents that create the problem of their utilization. The use of reverse osmosis and nanofiltration installations also has a serious drawback — the presence of concentrates that need to be disposed of. Currently, there is a research underway to develop technologies that allow reducing the costs of concentrates of reverse osmosis installations [11-19]. The use of the traditional approaches to solving the problems of drinking water supply in
a whole district (as in the case of New Moscow) described above leads to the need to solve a number of different problems related to the selection of units, their assembly, installation, repair, depending on the composition of the source water. In the present work, we have attempted to propose a new technological approach developed for the water supply department of the MGSU to solve the problem of drinking water supply [20-22]. A new approach to the purification of well water for drinking purposes is the use of universal membrane units. Regardless of the composition of the water (the presence or absence of high iron content, hardness ions, fluorides, ammonium, strontium in it), typical units are used for its purification, operating and servicing according to a single technological scheme. The difference is only in setting up the units onsite (choosing the values of the filtrate output and working pressure). A distinctive feature of the new units is the availability in the scheme of a special recycling unit (reduction of the concentrate volume). Fig. 4 shows the installation scheme with a capacity of 4-5 m3/h and its appearance.
Source water is supplied by the pump to the membrane apparatus 5 (Fig. 4). Here it is divided into 2 streams: filtrate and concentrate. Effective purification of water is achieved with a certain value of the filtrate output (it is chosen on the basis of experimental results or computer calculations). In order to reduce the consumption of the concentrate (up to 90-95 % of the filtrate output), membrane apparatus-concentrators of the second stage are used. Concentrate entering the apparatus-concentrators is also divided into a second stage filtrate and a second stage concentrate. The filtrate of the second stage is mixed with the source water. Thus, in order to achieve a higher value of the filtrate output, additional capital expenditures (for second-stage devices) and operating costs (for their chemical washing)
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Fig. 3. Technological scheme for the purification of well water (deferrization, removal of hydrogen sulfide, softening, removal of fluoride, strontium, ammonium, arsenic, desalination) using membrane technologies of nanofiltration or reverse osmosis:
I — water tower; 2 — degasser (aerator); 3 — feed pump; 4 — cartridge; 5 — working pump of high pressure; 6 — membrane modules; 7 — a tank of clean water; 8 — second lifting pumps; 9 — chlorinator; 10 — dosing system for the sludge inhibitor;
II — acidification system (for removal of hydrogen sulphide); 12 — purified water
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Fig. 4. Technological scheme of well water treatment with the use of membrane technologies of nanofiltration or reverse osmosis with a productivity of 4-5 m3/h and its appearance: 1 — mesh pre-filter (100 microns); 2 — inhibitory cartridge; 3 — centrifugal multi-stage pump; 4 — manometer; 5 — membrane element; 6 — the regulating valve; 9 — ball valve of the shut-off of the pump; 18 — bypass volume meter; 19 — hub device
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are required. Capital costs for installation depend on the type of membranes used (nanofiltration or reverse osmosis), having different values of specific permeability and working pressure.
The main technological difference between the developed membrane units from other systems:
1. Low water consumption for "own needs" (5-10 % of total consumption).
2. Simplicity of the apparatus (consists only of the pump and membrane units). Small size. Absence of reagents and consumables.
3. The unit is maintained only through conducting chemical rinsing of the membranes. Washings are carried out by personnel in accordance with the instructions once a year or less, depending on the composition of the treated water.
4. The economic advantage of the units is the absence of costs for reagents, waste materials, in reducing the cost of repairs, for discharging water into the sewage system, in reducing the cost of capital and the cost of the premises.
5. The economic advantage of the developed systems is demonstrated not only in comparison with technological schemes including reverse osmosis systems, but also with "classical" de-ironing schemes for catalytic loading, as well as de-ironing and sodium zeolite softening process, achieved due to cost savings for consumables materials, discharge into the sewer, repair and maintenance.
The ones shown in Fig. 4 serially produced units with a capacity of 5 m3/h are placed in block-boxes and used in units with a capacity of 5-20 m3/h.
MATERIALS AND METHODS
Selection of operating parameters of membrane units is based on the determination of the filtrate output at the first stage of the membrane unit. Depend-
ing on the filtrate output (the ratio between the filtrate consumption and the consumption of the source water entering the treatment), the composition of the purified water and the efficiency (selectivity) of the membranes are changed to purify from various impurities in the ionic form (fluoride ions, calcium ions, ions of strontium, etc.). The larger the filtrate output, the higher the concentrations of ions contained in the water in the channels of the apparatus and in the purified water become. The efficiency of water purification using various nanofiltration membranes, depending on the filtrate output, can be determined experimentally. Based on the results of the constructed experimental dependencies, the type of membrane optimal for the given case is chosen, which ensures minimum costs for cleaning with a given quality of purified water. When estimating the operating costs for cleaning, the values of the rates of formation of precipitates of slightly water-soluble salts (mainly calcium carbonate), determined experimentally, should also be used. The scheme of the experimental stand and its general appearance are shown in Fig. 5.
The source water is placed in the source water tank, from where it is supplied by the pump to the membrane apparatus. In the membrane apparatus, the feed water is separated into a filtrate and a concentrate. The filtrate (purified water) is collected in a filtrate tank, and the concentrate is returned to the source water tank. Thus, during the operation of the unit, the volume of water in the source water tank is constantly decreasing; from the tanks of the source water (concentrate) and the filtrate, water samples are taken in which the concentrations of dissolved salt ions are determined. Fig. 6, a, b, c show graphs of the experimental dependences of the concentrations of various contaminants removed from the water on the multiplicity of the decrease in the volume of source water in the tank 1 (Fig. 5) of the experimental unit (Fig. 5). The magnitude of the reduction in volume is defined as the ratio of the volume of
Fig. 5. The scheme of the experimental stand: 1 — source water tank; 2 — the tank for collecting the filter; 3 — nanofiltration apparatus; 4 — manometer; 5 — pressure control valve; 6 — pump
water in the source water tank 1 at the beginning of the experiment and at the time of sampling. Graphs of the experimental dependencies presented in Fig. 6 make it possible to choose the maximum value of the magnitude of the decrease in the volume of the source water (and, correspondingly, the filtrate output) for the given water composition. In the experiments, three types of well water used for drinking water supply in the Podol-sky district of New Moscow were used. The composition of the source water is shown in Table 1.
RESULTS OF THE RESEARCH
Fig. 6, a shows the dependences of the content in the water purified of fluoride ions on the multiplicity of the decrease in the volume of the source water in the experiments.
For the purification of water (composition 3, table 1), two types of membranes were used: nanofiltration membranes of 70 NE with a selectivity of 70 % and membranes of 90 NE with a selectivity of 90 %. The use of membranes with different selectivities allows, as will be shown below, to select the optimal operating mode of the water treatment unit. In Fig. 6, b and 5, c analogous dependences of the content of iron and calcium ions in water are presented.
On each graph, parallel to the abscissa axis, there passes a line corresponding to the maximum permissible concentration of the given ion in the purified water. The intersection of the graph of the experimentally obtained dependence with this line presents the value of the maximum permissible rate of the reduction in volume. Thus, Fig. 5, b shows the experimentally determined dependence of the concentration of iron in the filtrate on the multiplicity of the volumetric concentration of the initial water in the unit. As the graph implies, the concentration of iron in the filtrate of the unit reaches a value of 0.3 mg/L with a filtrate output of 0.67 (for a volume concentration amounting to 3). The choice of membrane characteristics has a significant value on the amount of operating costs [23]. As the experience of operating membrane units in the purification of well water shows, membrane selectivity affects not only the composition of purified water and the purification efficiency, but also the cost of service activities. The lower the selectivity of membranes, the less is the intensity of formation of precipitates of slightly soluble salts on membranes [24, 26-28]. Fig. 7 shows the curves of the dependence of the rates of formation on calcium carbonate precipitation membranes on the magnitude of the decrease in volume in the treatment of water of composition 3 (Table 1) using various membranes and inhibitory substances.
Determination of rates of calcium carbonate precipitation in membrane apparatus was carried out using the experimental bench shown in Figure 3 in ac-
Indicators Composition 1 (membrane 70 NE, CSM Korea) Composition 2 (membrane 70 NE, CSM Korea) Composition 3 (membrane 90 NE, CSM Korea)
Source Filtrate Concentrate Source Filtrate Concentrate Source Filtrate Concentrate
Calcium, mg-equ/L 3.5 1.2 12.7 8.5 3.0 28.5 8.0 1.5 7.5
Magnesium, mg-equ/L 1.0 0.4 3.6 2 0.7 7.0 2.0 0.3 7.1
Sodium + Potassium, mg-equ/L 1.0 0.5 3.0 1.5 0.7 4.4 2.0 0.5 6.5
Chlorides, mg-equ/L 1.5 0.7 4.5 4.0 1.8 12.4 4.0 1.0 13
Sulphates, mg-equ/L 1.0 0.35 3.8 1.5 0.5 5.9 2.0 0.3 7.1
Alkalinity, mg-equ/L 2.0 0.95 4.0 6.5 2.1 21.6 6.0 1.0 21.0
Iron total, mg/L 3.5 0.25 4.0 1.0 0.12 3.9 1.0 0.1 4.1
Fluorides, mg/L — — — — — — 3.0 0.7 9.5
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Table 1. The main chemical indicators of the investigated well water and water after treatment in container nanofiltration installations
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Fig. 6. Dependence of the following content: a — ion fluoride on the multiplicity of concentration; b — iron ions on the multiplicity of concentration; c — ions of calcium from the multiplicity of concentration
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Fig. 7. The results of the determination of the effectiveness of inhibitors produced by the company "Malotonazhnaya Khimiya" to prevent the formation of calcium carbonate precipitations in reverse osmosis membrane apparatus in the treatment of Moscow tap water, where: MA/AA — copolymer of maleic and acrylic acids (China); PASP — polyaspartate (Russia); PAK-4 — polyacrylic-lat (Russia); PESH — sodium polynoxy-succinate (China); PAAS — sodium salt of polyacrylic acid (China); PASP — polyaspartate (China): a — an increase in the amount of calcium carbonate precipitate, depending on the filtrate output of the membrane unit; b — dependence of growth rates of calcium carbonate precipitate in the presence of various inhibitors; c — the recommended working time of the unit between the conduct of chemical washes, depending on the values of the growth rates of the calcium carbonate precipitate
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cordance with the method developed by the authors earlier [21, 24, 25]. Table 1 also shows the values of the main indicators of the chemical composition of purified water and concentrate at a value of the multiplicity of volume concentration of 4, using different membranes. Forecasts of the compositions of purified water and concentrate were made on the basis of the program developed by the authors [24]. As already mentioned above, in order to reduce the consumption of concentrate in new developments, special additional membrane apparatus of the second stage are used (Fig. 5). Apparatus of the second stage are used to reduce the consumption of the concentrate by a factor of three to four compared with the consumption of the concentrate when the filtrate outputs are 0.67. Thus, the concentrate consumption will not exceed 5-10 % of the initial water consumption, which corresponds to the consumption of water for the needs of de-ironing facilities. Table 1 shows the compositions of the concentrate of the second stage with a multiplicity of a reduction in its volume by a factor of four, as well as the filtrate composition of the apparatuses of the second stage. It is of interest to study the dependence of the capital and operating costs of membrane units on the permissible value of the multiplicity of the volumetric concentration of the source water in the apparatus of the first stage, which determines the efficiency of purification from iron, hardness, fluorides and other contaminants. The
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change in capital costs when the permissible magnitude of the volume concentration multiplied is related to the cost of creating a second stage that provides a 10-times decrease in the volume of the concentrate and the use of different types of membranes with different values of specific productivity. Table 2 shows an example of the technological calculation of the unit: the determination of the compositions of the filtrate and concentrate at each stage of purification, the types of membranes used, and the determination of the necessary costs of the service reagents.
Calculations are made for water of composition 3 (Table 1) for a 10 m3/h installation. In order to determine the costs of service reagents produced by the company Traverse, the program developed at the Department of Water Supply and Sanitation of the MGSU [21, 24, 27] is used. The main technical and economic characteristics of membrane units with utilization of the concentrate (Fig. 3) with a capacity of 10 m3/h are shown in Table 3.
Depending on the composition of water (compositions 1 and 3, Table 1), the types of membranes in the first and second stages, the costs of service reagents, and energy consumption change. Calculations of operating costs included the determination of electricity costs for specified values of the filtrate output and determination of the costs of reagents (the cost of chemical washing, the cost and frequency of which increase
Table 2. An example of technological calculation of the unit. Determination of the compositions of the filtrate and concentrate of the unit at the 1 and 2 stages. Determination of the consumption of reagents (the Waterlab-Traverse program1) using the example of composition 3 (table1) for capacity setting of 10 m3/h
Indicators Source water SanPiN standards 1 stage 2 stage
filtrate concentrate filtrate concentrate
Membrane type 90 NE 8040 CSM (Korea) 70 NE 8040 CSM (Korea)
Filtrate output 0.75 0.75
The multiplicity of the decrease in the volume of water in the apparatus, K 4 4
Hardness, mg-equ/L 1-8 1-7 1.8 34.6 12.2 42.7
Calcium, mg-equ/L 8.0 — 1.5 27.5 8.9 34.6
Magnesium, mg-equ/L 2.0 — 0.3 7.1 2.3 8.1
Sodium + potassium, mg-equ/L 2.0 — 0.5 6.5 3.3 18.9
Chloride, mg-equ/L 4.0 10.0 1.0 13.0 6.7 20.1
Sulfates, mg-equ/L 2.0 10.0 0.3 7.1 2.4 8.9
Bicarbonate, mg-equ/L 6.0 — 1.0 21.0 5.4 31.6
Iron, mg/L 1.0 0.3 0.1 3.4 0.7 9.3
Fluorides, mg/L 3.0 1.5 0.7 12.3 2.8 9.1
Inhibitor Aminat K, dose, mg/l 3
Annual consumption 210
Estimated operating time before washing, h 650 510
Annual consumption of cleaning solutions, kg/year 120/50 000
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with increasing source water hardness and the filtrate output). In the experiments, three compositions of well water with different contents of iron, hardness, fluorides were used. Tables 3 and 4 show the results of calculations of the operational, capital and reduced costs (taking into account the discharge of the concentrate into the canalization) of the 7 water treatment units for the use of membrane units in the "classic" form with the output of the concentrate into the sewer (Table 3) and the application of new developed units with utilization of the concentrate (Table 4) with a capacity of 10 m3/h.
In order to confirm the effectiveness of the developed solutions, we compared the developed units with the facilities offered by the best-known companies on
the domestic market (Mediana-Filter, Helios Star, Eko-dar), they are presented in Fig. 8, 9, 10, respectively.
Economic comparison was made by comparing the values of the reduced costs [29]. In order to determine the values of these costs, the technical and commercial proposals provided by these companies were used to create water purification units with compositions 1, 2 and 3 with a capacity of 10 m3/h. Tables 4, 5 and 6 present the results of determining the values of capital, operating and reduced costs of facilities proposed by various domestic companies and comparing these indicators with the economic indicators of nanofiltration units developed at the Department of Water Supply and Sanitation.
Table 3. The main technical and economic parameters of the unit with a capacity of 10 m3/h. Washing (VPSM 5-16-2) with the cost of utilization of concentrate
Characteristics Composition of well water
1 3
Performance, m3/h 10 10
Water consumption for own needs, m3/h 0.6 0.6
Working pressure, bar 10 10
Performance of the main system, m3/h 10 10
Performance of the concentrate utilization system, m3/h 2.4 4.4
Type of membranes in the main system 90 NE CSM (Korea) 90 NE CSM (Korea)
Type of membranes in the utilization system 70 NE CSM (Korea) 70 NE CSM (Korea)
Cost of equipment in a container, rubles 2 100 000 2 400 000
Operating costs:
Electricity consumption, kW • h/rubles/year* 5.1/185 000 5.8/220 000
Replacement of membranes, rubles/year 80 000 118 000
Inhibitor: dose, mg/l/rubles/year — 1/7 000
Washing solutions: kg/year/rubles/year 48/20 000 96/40 000
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Table 4. Technical and economic comparison of costs of de-ironing of well water (treatment of water composition 1, Table 1) using various technologies (Fig. 1, 2)
Expenditures Offers from the company Helios Star Technology of the department
Types of basic equipment Deferrization filters Wave Cyber Nanofiltration system
Discharge into the sewer
The cost of the main equipment in the container, rubles 273 000.00 2 100 000.00
Operating costs: electricity, kW/rubles/year Consumables: Birm Inhibitor (Aminat K) Washing solutions, rubles/year Replacement of membranes 70 NE Sodium hypochlorite 2.5/60 000 rubles 98 kg/year / 20 000 rubles 3 kg/year / 2400 rubles/year 4,66/1 150 000 50 kg/year / 15 000 rubles 60 kg/year / 25 000 rubles 70 000 rubles/year
Total 82 400 205 000
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Table 5. Technical and economic comparison of the costs of removal of water hardness + iron (water treatment of the composition of 2, Table 1.) using various technologies (Fig. 3, 9)
Composition of expenditures Offers from the company "Mediana Filter" (Fig. 8, c) Technology of the department
Types of equipment, scheme Mechanical filtration, sorption, ionexchange filter Nanofiltration
Discharge into the sewer 1.44 m3/rubles
The cost of the main equipment, rubles 3 276 811.00 2 400 000.00
Operating costs: Electricity Consumables: Sodium chloride Inhibitor, 2 mg/l Washing solutions Coagulant Sodium hypochlorite Strong-acid cation resin in Na-form 9.7 kW/h / 210 000.00 rubles 524 000 rubles/year — 1872 kg/year 9 kg/year / 1200 rubles/year 11 kg/year / 2000 rubles/year 392 000 rubles/year / 60 kg 4.66 kW/h / 109 000.00 rubles 80 kg/year / 22 400 rubles 30 000 rubles/year
Total 773 200.00 161 400.00
Table 6. Technical and economic comparison of the costs of removal from the water of composition 3 (Table 1) of hardness, iron and fluorides using various water purification schemes (Fig. 4, 5, 10, 11)
Composition of expenditures Offers from the company "Ekodar" (Fig. 10) Offers from the company "Helios star" (Fig. 9) Technology of the Department of water Supply and sanitation
Types of equipment, scheme Pre-treatment system (deferrization) fine filter clarifying and sorption filter reverse osmosis unit Pre-treatment system (deferrization) Reverse osmosis system
Discharge flow rate, m3/h 2,9 3,6 0,6
Cost of equipment in container version 4 120 000 2 536 000 2 400 000
Operating costs: electricity, kW/h Consumables: BIRM Resin Washing solutions 10 190 000 rubles/year 6,8 130 000 rubles/year 5,66 110 000 rubles/year
Replacement of membranes 154/100 000 1 time in 2 years / 112 000 rubles —
Total 365 000.00 445 000.00 260 000.00
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The magnitude of the economic effect is obtained as the difference between the reported costs of installations, proposed in accordance with the "classical" technologies and units developed at the Department of Water Supply. The results of economic calculations show that even in the simplest case of well water purification from iron, the use of a nanofiltration system is economically more feasible than using traditional technologies based on aeration, catalytic oxidation and filtration. This is due to the constant cheapening and availability of membranes, low energy costs for membrane cleaning, the simplicity of the technological scheme, the small
size and compactness of the membrane systems. At the same time, the universality of nanofiltration systems in cleaning water from various contaminants makes it easy and affordable to simultaneously construct many water treatment systems and their maintenance within a single district.
CONCLUSIONS
Analysis of the dependencies of the filtrate quality on the filtrate output of membrane units with nano-filtration and reverse osmosis membranes shows that
all membranes effectively retard multivalent iron and calcium ions even at high rates of the filtrate output (0.75...0.9). The use of nanofiltration membranes with low selectivity can reduce the cost of electricity and reagents due to low rates of formation of precipitation of calcium carbonate on them. The use of universal membrane systems in container design for the purification of well water at a flow rate of 10 m3/h and above shows that even in the simplest cases (removal
of only iron from the water) the proposed technology demonstrates high economic and environmental effects compared to traditional technologies used for this purpose due to the simplicity, compactness, the absence of reagents and waste water. The use of universal units makes it easy to cover large areas with a large number of wells and consumers due to their construction, installation and maintenance in a single scheme.
REFERENCES
1. Lykins B.W., Clark R.M., Goodrich J.A. Point-of-use/point-of-entry for drinking water treatment. Levis, USA, 1993.
2. Rachwal A.J., Khow J., Colbourne J.S., O'Donnel J. Water treatment for public supply in the 1990's - A role for membrane technology? Desalination. 1994, vol. 97, issues 1-3, pp. 427-436. DOI:
£ ? 10.1016/0011-9164(94)00105-7.
3. Crittende J.C. Water Treatment: principles and
<£ design. 2nd ed. New Jersey, USA, John Wiley and Sons,
a ® 2005. 1968 p. u 3
> « 4. Al-Amoudi A.S. Factors affecting natural or-2 " ganic matter (NOM) and scaling fouling in NF mem? branes: A review. Desalination. 2010, vol. 259, no. 1-3,
M (U
§ pp. 1-10. DOI: 10.1016/j.desal.2010.04.003. § — 5. Garcia N.P., Rodriguez J., del Vigo F., Arm> strong M., Fazel M., Chesters S. Results of a neutral pH ot cleaner that removes complex fouling and metals from membranes. The international Desalination Association f £ World Congress — Sao Paolo, Brasil. REF: IDA 17 ! 1? WC-37930_PENA.
6. Salman M.A., AL-Nuwaibit G., Safar M., Alo >
g q Mesri A. Performance of physical treatment method 9 o and different commercial antiscalants to control scal-
g ing deposition in desalination plant. Desalination. Z £ 2015, vol. 369, no. 3, pp. 18-25. DOI: 10.1016/j.de-$ 1 sal.2015.04.023.
<u 7. Chaussemier M., Pourmohtasham E., Gelus D., ^ -2 Pecoul N., Perrot H., Ledion J. et al. State of art of natu-
Ol CO
^ g ral inhibitors of calcium carbonate scaling. A review
S § article. Desalination. 2015, vol. 356, pp. 47-55. DOI:
° J 10.1016/j.desal.2014.10.014.
en 8. Yangali-Quintanilla V.A., Dominiak D.M.,
z & van de Ven W. A smart optimization of antiscalant
ot T3 dosing in water. The International Desalination As-
g sociation World Congress — Sao Paolo, Brazil. REF:
2 IDA17WC-58252_Yangali-Quintanilla. • 9. Suratt W.B., Adrews D.R., Pujals V.J., Rich-
O 0 ards S.A. Design considerations for major membrane
S 2 treatment facility for groundwater. Desalination. 2000,
| ® vol. 131, no. 1-3, pp. 37-46. DOI: 10.1016/S0011-
x c 9164(00)90004-3. o In №
10. Bargeman G., Vollenbroek J.M., Straatsma J., Schroen C.G.P.H., Boom R.M. Nanofiltration of multi-component feeds. Interactions between neutral and charged components and their effect on retention. Journal of Membrane Science. 2005, vol. 247, issues 1-2, pp. 11-20. DOI: 10.1016/j.memsci.2004.05.022.
11. Potts D.E., Ahlert R.C., Wang S.S. A critical review of fouling of reverse osmosis membranes. Desalination. 1981, vol. 36, issue 3, pp. 235-264. DOI: 10.1016/S0011-9164(00)88642-7.
12. Her N., Amy G., Jarusutthirak C. Seasonal variations of nanofiltration (NF) foulants: identification and control. Desalination. 2000, issues 1-3, pp. 143-160. DOI: 10.1016/S0011-9164(00)00143-0.
13. Barlett M., Bird M.R., Howell J.A. An experimental study for the development of qualitative membrane cleaning model. Journal of Membrane Science. 1995, vol. 105, issues 1-2, pp. 147-157. DOI: 10.1016/0376-7388(95)00052-E.
14. Niewersch C., Zayat-Vogel B., Melin T., Wessling M. Nanofiltration for sulphate elimination in groundwater affected by open coal mining. The conference book of the 6th IWA Specialist Conference on Membrane Technology for Water and Water Treatment, 4-7 October 2011, Aachen, Germany. 2011, pp. 151-157.
15. Dale L.R., Reumundo T. Prototype testing facility for two-pass nanofiltration membrane seawater desalination process. AWWA, Membrane technology conference proceeding. 2005.
16. Segev R., Hasson D., Semiat R. Improved high recovery brackish water desalination process based on fluidized bed air stripping. Desalination. 2011, vol. 281, pp. 75-79. DOI: 10.1016/j.desal.2011.07.043.
17. Harries R.C. A field trial of seeded reverse osmosis for desalination of a scaling-type mine water. Desalination. 1985, vol. 56, pp. 227-236. DOI: 10.1016/0011-9164(85)85027-X.
18. Veespareni S., Bond R. Getting this last drop: new technology for treatment of concentrate. Tianjin IDA World Congress 2013 on Desalination and Water Reuse, October 20-25, China 2013, TIAN 13-357.
19. Turek M., Mitko K., Piotrowski K., Dydo P., Laskovska E., Jakobic-Kolon A. Prospects for high water recovery membrane desalination. Desalination. 2017, vol. 401, pp.180-189. DOI: 10.1016/j.de-sal.2016.07.047.
20. Ventresque C., Gisclon V., Bablon G., Shagneau G. An outstanding feat of modern technology: the Mery-Sur-Oise Nanofiltration treatment Plant (340,000 m3/dcu.metr per day). Desalination. 2000, vol. 131, issues 1-3, pp. 1-16. DOI: 10.1016/S0011-9164(00)90001-8.
21. Pervov A.G. Scale formation prognosis and cleaning procedure schedules in reverse osmosis operation. Desalination. 1991, vol. 83, pp. 77-118. DOI: 10.1016/0011-9164(91)85087-B.
22. Pervov A.G., Andrianov A.P. Application of membranes to treat wastewater for its recycling and reuse: new considerations to reduce fouling and increase recovery up to 99 percent. Desalination and Water Treatment. 2011, vol. 35, pp. 2-9. DOI: 10/5004/ dwt.2011.3133.
23. Goodin B.D., Pinto J.M., Butow R.R. Back to the future: innovation and energy efficiency on a lowTDS BWRO retrofit/expansion. The International Desalination Association World Congress — Sao Paolo, Brazil. REF:IDA17WC-58359_ Goodin.
24. Pervov A.G. A simplified RO process design based on understanding of fouling mechanisms. Desali-
Received June 12, 2018.
Adopted in final form on July 17, 2018.
Approved for publication on July 31, 2018.
nation. 1999, vol. 126, issue 1-3, pp. 227-247. DOI: 10.1016/s0011-9164(99)00179-4.
25. Pervov A.G. Utilization of concentrate in reverse osmosis in water desalination systems. Tianjin IDA World Congress 2013 on Desalination and Water Reuse, October 20-25, China 2013, TIAN 13-216.
26. Pervov A.G. Precipitation of calcium carbonate in reverse osmosis retentate flow bymeans of seeded techniques - a tool to increase recovery. Desalination. 2015, vol. 368, pp. 140-151. DOI: 10.1016/j. desal.2015.02.024,368 (2015) 140-151.
27. Pervov A., Andrianov A., Rudakova G., Popov K. A comparative study of some novel "green" and traditional antiscalants efficiency for the reverse osmotic Black Sea water desalination. Desalination and Water Treatment. 2017, vol. 73, pp. 11-21. DOI: 10.5004/ dwt.2017.20363.
28. Pervov A., Andrianov A., Deposition of calcium and magnesium from RO concentrate by means of seed crystallization and production of softened water for techical purposes. Desalination and Water Treatment. 2018, vol. 110, pp. 10-18. DOI: 10.5004/ dwt.2018.21875. (2018) 1-9.
29. Pianta R., Boller M.M., Urfer D.D., Chap-paz A.A., Gmunder A.A. Costs of conventional versus membrane treatment for karstic spring water. Desalination. 2000, vol. 131, issues 1-3, pp. 245-255. DOI: 10.1016/S0011-9164(00)90023-7.
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About the authors: Yu Dan Su — director, RAIFIL China, CSM official representative in Russia,
RM 206. Chengwen Business Building, No. 4285 Shendu Road, Shanghai, China, raifil@yandex.ru; CSM official representative in Russia, Room 206, Cheng Wen Business Building, № 4285, Shen Du Rd, Ming Hang District, Shanghai, China 201112, raifil@yandex.ru;
Alexey G. Pervov — Doctor of Technical Sciences, Professor of the Department of Water Supply and Sanitation, Moscow State University of Civil Engineering (National Research University) (MGSU), 26 Yaroslavskoe shosse, Moscow, 129337, Russian Federation, waterlab@yandex.ru;
Vladimir A. Golovesov — post-graduate student of the Department of Water Supply and Sanitation, Moscow State University of Civil Engineering (National Research University) (MGSU), 26 Yaroslavskoe shosse, Moscow, 129337, Russian Federation, golovesov.vova@mail.ru.
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ЛИТЕРАТУРА
1. Lykins B.W., Clark R.M., Goodrich J. A. Point-of-use/point-of-entry for Drinking water treatment. Levis, USA, 1993.
2. Rachwal A.J., Khow J., Colbourne J.S., O'Donnel J. Water treatment for public supply in the 1990's — A role for membrane technology? // Desalination. 1994. Vol. 97. Issues 1-3. Pp. 427-436. DOI: 10.1016/0011-9164(94)00105-7.
3. Crittende J.C. Water Treatment: principles and design. 2nd ed. New Jersey, USA : John Wiley and Sons, 2005. 1968 p.
4. Al-Amoudi A.S. Factors affecting natural organic matter (NOM) and scaling fouling in NF membranes: A review // Desalination. 2010. Vol. 259. No. 1-3. Pp. 1-10. DOI: 10.1016/j.desal.2010.04.003.
ем
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5. Garcia N.P., Rodriguez J., del Vigo F., Armstrong M., FazelM., Chesters S. Results of a neutral pH cleaner that removes complex fouling and metals from membranes // The International Desalination Association World Congress — Sao Paolo, Brasil. REF: IDA 17 WC-37930_PENA.
6. Salman M.A., AL-Nuwaibit G., Safar M., Al-Mesri A. Performance of physical treatment method and different commercial antiscalants to control scaling deposition in desalination plant // Desalination, 2015. Vol. 369. No. 3. Pp. 18-25. DOI: 10.1016/j.de-sal.2015.04.023.
7. Chaussemier M., Pourmohtasham E., Gelus D., PecoulN., PerrotH., Ledion J. et al. State of art of natural inhibitors of calcium carbonate scaling. A review article // Desalination. 2015. Vol. 356. Pp. 47-55. DOI: 10.1016/j.desal.2014.10.014.
8. Yangali-Quintanilla V.A., Dominiak D.M., van de Ven W. A smart optimization of antiscalant dosing in water // The International Desalination Association World Congress — Sao Paolo, Brazil. REF:
? ? IDA17WC-58252_Yangali-Quintanilla.
9. Suratt W.B., Adrews D.R., Pujals V.J., Rich-« eo ards S.A. Design considerations for major membrane
0 § treatment facility for groundwater // Desalination. 2000. çjn Vol. 131. No. 1-3. Pp. 37-46. DOI: 10.1016/S0011-¿S m 9164(00)90004-3.
r
o q 10. Bargeman G., Vollenbroek J.M., Straatsma J.,
2 H Schroen C.G.P.H., Boom R.M. Nanofiltration of multi-
£ "¡5 component feeds. Interactions between neutral and
^ charged components and their effect on retention // Jour-
l' nal of Membrane Science. 2005. Vol. 247. Issues 1-2. Pp. 11-20. DOI: 10.1016/j.memsci.2004.05.022.
J.| 11. Potts D.E., Ahlert R.C., Wang S.S. A critical
0 ¿j review of fouling of reverse osmosis membranes // Decs ^ salination. 1981. Vol. 36. Issue 3. Pp. 235-264. DOI: g U 10.1016/S0011-9164(00)88642-7.
1 o
§ 12. Her N., Amy G., Jarusutthirak C. Seasonal
cn '<» variations of nanofiltration (NF) foulants: identification
ot and control // Desalination. 2000. Vol. 132. Issues 1-3.
— 5 Pp. 143-160. DOI: 10.1016/S0011-9164(00)00143-0.
m
.E 13. Barlett M., Bird M.R., Howell J.A. An ex-
St00 perimental study for the development of qualitative
co o membrane cleaning model // Journal of Membrane Sci-
9 8 ence. 1995. Vol. 105. Issues 1-2. Pp. 147-157. DOI:
g ^ 10.1016/0376-7388(95)00052-E.
to 14. Niewersch C., Zayat-Vogel B., Melin T., ^ c Wessling M. Nanofiltration for sulphate elimination in _ $ groundwater affected by open coal mining // The cones ference book of the 6th IWA Specialist Conference on ^ Membrane Technology for Water and Water Treatment, $ => 4-7 October, Aachen, Germany. 2011. Pp. 151-157. g (9 15. Dale L.R., Reumundo T. Prototype testing fa-k ® cility for two-pass nanofiltration membrane seawater
1 ë desalination process // AWWA, Membrane technology o "S conference proceeding. 2005.
(0 £
16. Segev R., Hasson D., Semiat R. Improved high recovery brackish water desalination process based on fluidized bed air stripping // Desalination. 2011. Vol. 281. Pp. 75-79. DOI: 10.1016/j.desal.2011.07.043.
17. Harries R.C. A field trial of seeded reverse osmosis for desalination of a scaling-type mine water // Desalination. 1985. Vol. 56. Pp. 227-236. DOI: 10.1016/0011-9164(85)85027-X.
18. Veespareni S., Bond R. Getting this last drop: new technology for treatment of concentrate // Tianjin IDA World Congress 2013 on Desalination and Water Reuse, October 20-25, China 2013, TIAN 13-357.
19. TurekM., Mitko K., Piotrowski K., Dydo P., Laskovska E., Jakobic-Kolon A. Prospects for high water recovery membrane desalination // Desalination. 2017. Vol. 401. Pp.180-189. DOI: 10.1016/j.de-sal.2016.07.047.
20. Ventresque C., Gisclon V., Bablon G., Shag-neau G. An outstanding feat of modern technology: the Mery-Sur-Oise Nanofiltration treatment Plant (340,000 m3/d) // Desalination. 2000. Vol. 131. Issues 1-3. Pp. 1-16. DOI: 10.1016/S0011-9164(00)90001-8.
21. Pervov A.G. Scale formation prognosis and cleaning procedure schedules in reverse osmosis operation // Desalination. 1991. Vol. 83. Issues 1-3. Pp. 77118. DOI: 10.1016/0011-9164(91)85087-B.
22. Pervov A.G., Andrianov A.P. Application of membranes to treat wastewater for its recycling and reuse: new considerations to reduce fouling and increase recovery up to 99 percent // Desalination and Water Treatment. 2011. Vol. 35. Pp. 2-9. DOI: 10/5004/ dwt.2011.3133.
23. Goodin B.D., Pinto J.M., Butow R.R. Back to the future: innovation and energy efficiency on a lowTDS BWRO retrofit/expansion // The International Desalination Association World Congress — Sao Paolo, Brazil, REF:IDA17WC-58359_ Goodin.
24. Pervov A. A simplified RO process design based on understanding of fouling mechanisms // Desalination. 1999. Vol. 126. Issue 1-3. Pp. 227-247. DOI: 10.1016/s0011-9164(99)00179-4.
25. Pervov A. Utilization of concentrate in reverse osmosis in water desalination systems. Tianjin IDA World Congress 2013 on Desalination and Water Reuse, October 20-25, China 2013, TIAN 13-216.
26. Pervov A.G. Precipitation of calcium carbonate in reverse osmosis retentate flow bymeans of seeded techniques - a tool to increase recovery // Desalination. 2015. Vol. 368. Pp. 140-151. DOI: 10.1016/j. desal.2015.02.024.
27. Pervov A., Andrianov A., Rudakova G., Popov K. A comparative study of some novel "green" antiscalants efficiency for the reverse osmosis Black Sea Desalination // Desalination and Water Treatment. 2017. Vol. 73. Pp. 11-21. DOI: 10.5004/dwt.2017.20363.
28. Pervov A., Andrianov A. Deposition of calcium and magnesium from RO concentrate by means
of seed crystallization and production of softened water for technical purposes // Desalination and Water Treatment. 2018. Vol. 110. Pp. 10-18. DOI: 10.5004/ dwt.2018.21875.
29. Pianta R., Boiler M., Urfer D., Chappaz A., Gmunder A. Costs of conventional vs membrane treatment for karstic spring water // Desalination. 2000. Vol. 131. Issues 1-3. Pp. 245-255. DOI: 10.1016/ S0011-9164(00)90023-7.
Поступила в редакцию 12 июня 2018 г. Принята в доработанном виде 17 июля 2018 г. Одобрена для публикации 31 июля 2018 г.
Об авторах: Ю Дан Су — директор, «RAIFIL China», представитель компании CSM в России, 201112, Китай, Шанхай, р-н Мин Ханг, Шен Ду Роуд, 4285, Ченг Вен Бизнес Билдинг, оф. 206, raifil@yandex.ru;
Первов Алексей Германович — доктор технических наук, профессор кафедры водоснабжения и водо-отведения, Национальный исследовательский Московский государственный строительный университет (НИУ МГСУ), 129997, г. Москва, Ярославское шоссе, д. 26, waterlab@yandex.ru;
Головесов Владимир Алексеевич — аспирант кафедры водоснабжения и водоотведения, Национальный исследовательский Московский государственный строительный университет (НИУ МГСУ), 129997, г. Москва, Ярославское шоссе, д. 26, golovesov.vova@mail.ru.
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