SU948895A1

SU948895A1 - Method for processing waste liquors from iodine and bromine production

Info

Publication number: SU948895A1
Application number: SU802978420A
Authority: SU
Inventors: Чары Атабаевич Кулиев; Агамамед Ходжамамедов; Владимир Иванович Ксензенко; Худайберды Аннаев; Аллаберды Нурыев; Дмитрий Сергеевич Стасиневич; Огульшекер Овезова
Original assignee: Институт химии АН ТССР
Priority date: 1980-09-12
Filing date: 1980-09-12
Publication date: 1982-08-07

Description

Изобретение относится к способам переработки отработанных сточных вод йодобромных производств, использующих в качестве сырья подземные рассолы (буровые воды), которые содержат значительные концентрации хлоридов натрия, кальция, магния и калия и, кроме того, бор, литий и стронций.The invention relates to methods for processing wastewater from iodine-bromine production using underground brines (drilling water), which contain significant concentrations of sodium, calcium, magnesium and potassium chlorides and, in addition, boron, lithium and strontium.

Наиболее близким к предлагаемому 1° по технической сущности и достигаемому результату является способ переработки отработанных сточных вод йодобромных производств, включающий выделение микроэлементов и гидроокиси магния. Согласно этому способу воду подщелачивают для соосаждения микроэлементов совместно с гидроокисью магния. Из полученного осадка rtocne соответствующих химических обработок получают химическое удобрение, содержащее бор, йод, железо, магний, марганец, медь и другие £1].Closest to the proposed 1 ° in technical essence and the achieved result is a method of processing waste wastewater of iodine-bromine production, including the allocation of trace elements and magnesium hydroxide. According to this method, water is alkalinized to co-precipitate trace elements together with magnesium hydroxide. A chemical fertilizer containing boron, iodine, iron, magnesium, manganese, copper and others £ 1] is obtained from the obtained rtocne precipitate of the corresponding chemical treatments.

Однако данным способом не решаются вопросы комплексного извлечения всех полезных компонентов, содержащихся в отработанной воде.However, this method does not solve the issues of integrated extraction of all useful components contained in waste water.

Цель изобретения - комплексное извлечение всех полезных компонентов, содержащихся в отработанной воде, создание безотходной технологии.The purpose of the invention is the comprehensive extraction of all useful components contained in the waste water, the creation of waste-free technology.

Поставленная цель достигается тем, что согласно способу, включающему выделение микроэлементов и гидроокиси магния, воду концентрируют до содержания солей 18-20% с отделением образовавшегося сульфата кальция, затем обрабатывают 15-20%-ным раствором щелочи до pH 3,5-4,0 извлечением бора ионообменом, после чего упаривают до плотности 1330-1340 кг/м^э и отделяют выпавший хлористый натрий, а раствор повторно упаривают до плотности 1430-1440 кг/м® с отделением выпавших магнезиальных солей - карналлита и тахгидрита, которые разла3 948895 гают путем смешения с исходной отработанной водой в равном соотношении с получением хлористого калия и маточного раствора, который присоединяют к раствору,оставшемуся после выделения магнезиальных солей, затем объединенный раствор обрабатывают 8-10%-ным раствором щелочи до pH 9,5~9,7 с отделением выпавшей гидроокиси магния, а раствор обрабатывают 2,5“4,0%-ной соляной кислотой до pH 7,0-7,5 и извлекают литий и стронций сорбцией, после чего раствор снова упаривают до плотности 1420-1425 кг/м³, отделяют выпавший хлористый натрий, а оставшийся 3840%-ный раствор хлористого кальция выпускают в виде товарного продукта.This goal is achieved by the fact that according to the method, including the allocation of trace elements and magnesium hydroxide, water is concentrated to a salt content of 18-20% with separation of the formed calcium sulfate, then treated with a 15-20% alkali solution to a pH of 3.5-4.0 extraction of boron by ion exchange, after which it is evaporated to a density of 1330-1340 kg / m ^e and the precipitated sodium chloride is separated off, and the solution is re-evaporated to a density of 1430-1440 kg / m® with separation of the precipitated magnesia salts - carnallite and tachhydrite, which decompose by 948895 confusion with the outcome waste water in equal proportions to obtain potassium chloride and the mother liquor, which is attached to the solution remaining after the separation of magnesian salts, then the combined solution is treated with an 8-10% alkali solution to a pH of 9.5 ~ 9.7 with separation of the precipitated hydroxide magnesium, and the solution is treated with 2.5 “4.0% hydrochloric acid to a pH of 7.0-7.5 and lithium and strontium are removed by sorption, after which the solution is again evaporated to a density of 1420-1425 kg / m ³ , the precipitate is separated sodium chloride, and the remaining 3840% solution of calcium chloride release They come in the form of a marketable product.

Переработка отработанных вод йодобромных производств основана на ступенчатом их испарении и подщелачивании с отделением последовательно выделяющихся компонентов.The treatment of wastewater from iodine-bromine production is based on their stepwise evaporation and alkalization with separation of sequentially released components.

Буровая вода перед извлечением из нее йода и брома для предотвра- ₂₅щёния их гидролиза подкисляется, поэтому отработанная вода имеет pH 2,63,0. На первой стадии отработанную воду концентрируют путем солнечного испарения в специально устроенных бассейнах до содержания солей 18-20%. На этой стадии отделяются механические примеси, отстаиваются кислые органические компоненты и осаждаются наибольшие количества сульфата кальция. Концентрированный рассол нейтрализуется 15-20%-ным раствором едкого натра до pH 3,5“4,0 и направляется на извлечение бора с помощью ионообменных смол. Низкая концентрация (меньше 16,0 мас?%) применяемой щелочи вызывает увеличение объема рассола, что приводит к уменьшению содержания бора, а высокая концентрация (больше 20,0 мас.%) - у-кристаллизацию хлористого натрия, что может отрицательно сказаться на сорбции бора. Оптимальное значение pH способа извлечения бора из этих вод 3,5-4,0. После извлечения бора рассол направляется на дальнейшее упаривание в естественных или заводских условиях, которое продолжают До достижения плотности 1330-1340 кг/м³. При этом в осадок выпадает до 9295% содержащегося в рассоле хлористого натрия. Его отделяют, промывают раствором хлбристого натрия, сушат и выпускают в качестве товарного продукта. Промывные воды после трехкратного использования присоединяют к маточному раствору и направляют на дальнейшее упаривание, которое ведут до плотности 1430-1440 кг/м³. При этом осаждаются магниевые соли (КСЕ* *МдС(?<2*6Н<20) и тахгидрит (гИдСе^ *СаСЕ_гх1гН^О). Их отделяют и обрабатывают на холоду исходной отработан10 ной водой в отношении 1:1, при этом до 60-70% х'лористого калия, содержащегося в солевой смеси, остается в виде твердого осадка, который отделяют, сушат и выпускают в виде то15 варного продукта. .Изменение значений указанных отношений уменьшает выход хлористого калия.Drilling water before removing it from iodine and bromine schoniya ₂₅ to prevent hydrolysis of acidified waste water therefore has pH 2,63,0. In the first stage, the waste water is concentrated by solar evaporation in specially designed pools to a salt content of 18-20%. At this stage, mechanical impurities are separated, acidic organic components are sedimented and the greatest amounts of calcium sulfate are precipitated. The concentrated brine is neutralized with a 15-20% sodium hydroxide solution to a pH of 3.5–4.0 and is directed to boron recovery using ion-exchange resins. A low concentration (less than 16.0 wt.%) Of the alkali used causes an increase in the volume of brine, which leads to a decrease in the boron content, and a high concentration (more than 20.0 wt.%) Causes the γ-crystallization of sodium chloride, which can adversely affect sorption boron. The optimal pH of the method for extracting boron from these waters is 3.5-4.0. After boron extraction, the brine is sent for further evaporation in natural or factory conditions, which is continued until the density reaches 1330-1340 kg / m ³ . In this case, up to 9295% of sodium chloride contained in the brine precipitates. It is separated, washed with a solution of sodium chloride, dried and released as a commercial product. Wash water after three use is attached to the mother liquor and sent for further evaporation, which lead to a density of 1430-1440 kg / m ³ . Magnesium salts (KCE * * MdC (? <2 * 6H <20) and tachyhydrite (gIdCe ^ * CaCE _g x1gH ^ O) are precipitated. They are separated and treated in the cold with the original waste water in a ratio of 1: 1, while up to 60-70% of potassium chloride contained in the salt mixture remains in the form of a solid precipitate, which is separated, dried and released as a finished product. Changing the values of these ratios reduces the yield of potassium chloride.

Маточный раствор после разложения соединяют с маточником, оставшимся после отделения магнезиальных солей, и соединенный раствор обрабатывают 8-10%-ным раствором едкого натра до pH 9>5“9,7 (или θΝαοΗ ⁼ = 1:1,75) для осаждения гидроокиси магния. Выпавшую гидроокись магния отделяют и прокаливают для получения товарной окиси магния. Степень извле· чения магния при этом 96-98%. Меньше 8% применяемой щелочи увеличивает объем обрабатываемых вод, а выше 10% замедляет процесс осаждения гидроокиси магния в связи с ухудшением диффузионных процессов. Повышение- pH от указанного предела вызывает осаждение гидроокисью кальция и стронция, а понижение его уменьшает степень извлечения магния из рассола, что приводит к ухудшению качества получаемых продуктов. МаточЗА ν ” ныи раствор после отделения гидроокиси магния нейтрализуют 2,5^_4,0%-ной соляной кислотой до pH 7,07,5· Низкая концентрация (ниже 2,5%) применяемой кислоты приводит к уве^4S личению объема перерабатываемых вод, а высокая концентрация (больше 4,0%)к увеличению содержания хлористого натрия в рассоле*и выделению его в твердую фазу, что является нежела50 тельным для сорбционных процессов. После извлечения лития и стронция сорбционным способом рассол⁴ направляют на дальнейшее упаривание до плотности 1420-1425 кг/м³. При этом 55 95“97% содержащегося хлористого натрия выпадает в осадок, который отделяют, промывают раствором хлористого натрия, сушат и выпускают в виде то5 948895 верного продукта. Маточный раствор, содержащий 39”30% хлористого кальция , выпускается в виде товарного продукта.The mother liquor after expansion is combined with mother liquor remaining after separation of the magnesium salt solution is treated with and connected 8-10% solution of sodium hydroxide to pH 9> 5 "9.7 (or θΝαοΗ ^{= =} 1: 1.75) to precipitate hydroxide magnesium. The precipitated magnesium hydroxide is separated and calcined to obtain salable magnesium oxide. The degree of extraction of magnesium is 96-98%. Less than 8% of the alkali used increases the volume of treated water, and above 10% it slows down the deposition of magnesium hydroxide due to the deterioration of diffusion processes. Increasing the pH from the specified limit causes precipitation of calcium hydroxide and strontium, and lowering it reduces the degree of extraction of magnesium from brine, which leads to a deterioration in the quality of the resulting products. After a separation of magnesium hydroxide, Matroza ν ”solution is neutralized with 2.5 ^_ 4.0% hydrochloric acid to pH 7.07.5. A low concentration (below 2.5%) of the acid used leads to an increase in the volume of the treated water, ^4S and a high concentration (more than 4.0%) leads to an increase in the content of sodium chloride in brine * and its release into the solid phase, which is undesirable for sorption processes. After extraction of lithium and strontium by the sorption method, brine ^{4 is} sent for further evaporation to a density of 1420-1425 kg / m ³ . In this case, 55 95 “97% of the contained sodium chloride precipitates, which is separated off, washed with a solution of sodium chloride, dried and released in the form of a true product. The mother liquor containing 39 ”30% calcium chloride is available as a commercial product.

Таким образом, переработка отра- 5 ботанных вод йодобромных производств позволяет получать раствор хлористого кальция, гипс, хлористый натрий, хлористый калий, окись магния, а также концентраты для получения бора, 10 лития и стронция при благоприятных условиях извлечения последних из вод.Thus, the processing of the treated water from iodine-bromine production allows one to obtain a solution of calcium chloride, gypsum, sodium chloride, potassium chloride, magnesium oxide, as well as concentrates for the production of boron, 10 lithium and strontium under favorable conditions for the extraction of the latter from water.

П р и м е р; Отработанная вода· йодобромного производства, имеющая 15 состав, мас.%: NaCE 9»71; СаС₽<^ 2,00; МдСЕ^ 0,40; CaS04 0,06; КСЕ 0,09; Псолей 12,25; 0,02; Li 0,0004 и Sr 0,030 и pH 2,6, концентрируется в испарителе до содержания солей 20%, _мпричем предварительно очищается от механических примесей, из нее отстаиваются кислые органические компоненты и выпадает гипс. Осветленный рассол нейтрализуют 20%-ным раство- ₂₅ром едкого натра до pH 4,0 и направляют на извлечение бора с помощью ионнообменйых смол. Освобожденный от бора рассол направляется во второй испаритель где концентрируется до ₃₀ плотности 1330 кг/м³, причем 95% хлористого натрия, содержащегося в рассоле, выпадает в твердую фазу, остаток отделяют, промывают раствором хлористого натрия и сушат. Промывные воды после трехкратного использования возвращают во второй испаритель . Маточный раствор подвергают дальнейшему концентрированию в третьем испарителе до плотности 1440 кг/м³при этом из него осаждаются карналлит и тахгидрит. Осадок отделяют и разлагают на холоду исходной отработанной водой при соотношении 1:1, при этом около 70% содержащегося в осадке хлористого калия остается в твердой фазе. Его отделяют от раствора и сушат. Промывной раствор, содержащий в основном хлориды кальция и магния, объединяют с маточным раствором и обрабатывают 10%-ным раствором едкого натра при pH 9,6, при этом осаждается гидроокись магния. Расход щелочи составляет 175% от теорерического, степень извлечения магния 98%. Гидроокись магния отделяют от раствора и прокаливают для получения окиси магния. Маточный раствор после осаждения гидроокиси магния нейтра лизуют 2,5%^_ной соляной кислотой до pH 7,0. Полученный рассол, содержащий 23% солей и имеющий плотность 1210 кг/м³, направляется на извле- чение лития и стронция (9) сорбционным методом. После извлечения этих компонентов рассол упаривают в четвертом испарителе,где из него выпаflaet в твердую фазу 96% содержащегося хлористого натрия, промывают раствором хлористого натрия и сушат. Маточный рассол, имеющий плотность 1420 кг/м³ и содержащий 40% хлористого кальция, выпускают в качестве товарного продукта.PRI me R; Wastewater · iodine-bromine production, having 15 composition, wt.%: NaCE 9 "71; CaC $ <^ 2.00; MdCE ^ 0.40; CaS04 0.06; KSE 0.09; Psoley 12.25; 0.02; Li 0.0004 and Sr 0.030 and pH 2.6, are concentrated in the evaporator to a salt content of 20%, _m and pre-cleaned of mechanical impurities, acidic organic components are settled from it and gypsum precipitates. The clarified brine is neutralized with 20% rum dissolving ₂₅ of sodium hydroxide to pH 4,0 and sent for recovery of boron via ionnoobmenyyh resins. The brine freed from boron is sent to a second evaporator where it is concentrated to _{30 with a} density of 1330 kg / m ³ , with 95% of the sodium chloride contained in the brine falling into the solid phase, the residue is separated, washed with a solution of sodium chloride and dried. Wash water after three use is returned to the second evaporator. The mother liquor is further concentrated in the third evaporator to a density of 1440 kg / m ³ while carnallite and tachyhydrite are precipitated from it. The precipitate is separated and decomposed in the cold with the original waste water at a ratio of 1: 1, while about 70% of the potassium chloride contained in the precipitate remains in the solid phase. It is separated from the solution and dried. The washing solution, which contains mainly calcium and magnesium chlorides, is combined with the mother liquor and treated with a 10% sodium hydroxide solution at pH 9.6, and magnesium hydroxide precipitates. Alkali consumption is 175% of theoretical, the degree of extraction of magnesium is 98%. Magnesium hydroxide is separated from the solution and calcined to obtain magnesium oxide. The mother liquor after the precipitation of magnesium hydroxide neutrals lizuyut ^_ 2.5% hydrochloric acid to pH 7,0. The resulting brine containing 23% salts and having a density of 1210 kg / m ³ is sent to the extraction of lithium and strontium (9) by the sorption method. After the extraction of these components, the brine is evaporated in the fourth evaporator, where 96 ml of the sodium chloride contained in the solid is precipitated from it, washed with a solution of sodium chloride and dried. Royal brine, having a density of 1420 kg / m ³ and containing 40% calcium chloride, is released as a commercial product.

Таким образом, при переработке 1 т отработанной буровой воды получают, кг: гипс 0,5; хлористый натрий 99; хлористый калий 0,6; окись магния 1,6; 40%-ный раствор хлористого кальция 51, а также концентраты, с содержанием, %·. борный ангидрид 0,03; литий 0,008 и странций 0,4. По этим компонентам достигается обогащение соответственно в 1,6;-13 и 12 раз и создаются благоприятные условия для извлечения их сорбционными способами. Расход реагентов на 1 т отработанной воды составляет, кг:едкий натр 5,9; соляная кислота (в расчете на 100% НСЕ) 0,8; пресная вода 34 кг.Thus, in the processing of 1 ton of waste drilling water receive, kg: gypsum 0.5; sodium chloride 99; potassium chloride 0.6; magnesium oxide 1.6; 40% solution of calcium chloride 51, as well as concentrates, with a content,% ·. boric anhydride 0.03; lithium 0.008 and stratum 0.4. For these components, enrichment is achieved 1.6, 13 and 12 times, respectively, and favorable conditions are created for their extraction by sorption methods. The consumption of reagents per 1 ton of waste water is, kg: caustic soda 5.9; hydrochloric acid (based on 100% NSE) 0.8; fresh water 34 kg.

Технико-экономическая эффективность способа состоит в возможности комплексной переработки отработанных вод с извлечением всех полезных компонентов, исключении сброса этих вод и решении тем самым экологических проблем.The technical and economic efficiency of the method consists in the possibility of complex processing of waste water with the extraction of all useful components, eliminating the discharge of these waters and thereby solving environmental problems.

Claims

The invention relates to methods for processing wastewater from iodine-bromine production, using underground brines (drilling waters) as raw materials, which contain significant concentrations of sodium, calcium, magnesium and potassium chlorides, and boron, lithium and strontium. The closest to the proposed technical essence and the achieved result is a method of processing waste wastewater iodine-bromine production, including the release of trace elements and magnesium hydroxide. According to this method, water is alkalinized to co-precipitate trace elements together with magnesium hydroxide. Chemical fertilizers containing boron, iodine, iron, magnesium, manganese, copper and other flJ are obtained from the obtained rtocne precipitate of the corresponding chemical treatments. However, this method does not solve the issues of complex extraction of all useful components that are contained in the waste water. The purpose of the invention is the complex extraction of all useful components contained in the waste water, the creation of non-waste technology. The goal is achieved by the fact that according to the method, including the extraction of trace elements and magnesium hydroxide, water is concentrated to a salt content of 18–20% with the separation of calcium sulfate formed, then treated with a 15–20% alkali solution to a pH of 3.5–, p extracting boron by ion exchange, after which it is evaporated to a density of 1330-UtO kg / m and the precipitated sodium chloride is separated, and the solution is re-evaporated to a density of 1 30 30-1 40 kg / m with the separation of the precipitated magnesia salts — carnallite and hydrochloride, which are decomposed by mixing from the original equal in proportion to the production of potassium chloride and the mother liquor, which is added to the solution remaining after the separation of the magnesium salts, then the combined solution is treated with an alkali solution to a pH of 9.5-9.7 with separation of precipitated magnesium hydroxide, and the solution is treated 2.5.0% hydrochloric acid to pH 7.0-7.5 and lithium and strontium are removed by sorption, after which the solution is again evaporated to a density of kg / m, the precipitated sodium chloride is separated, and the remaining 38401 solution calcium chloride is released in the form ary Product Recycling wastewater iodine bromine production is based on their stepwise alkalization and evaporation with separation consistent propelling isolated components. Before extracting iodine and bromine from it, water is acidified to prevent their hydrolysis; therefore, the waste water has a pH of 2, 3.0. In the first stage, the waste water is concentrated by solar evaporation in specially arranged pools to a salt content of 18–20. At this stage, mechanical impurities are separated, acidic organic components are settled, and the greatest amounts of calcium sulfate are precipitated. The concentrated brine is neutralized with a solution of sodium hydroxide to pH 3, O, and is directed to the extraction of boron using ion exchange resins. The low concentration (less than 16.0 May;) of the alkali used causes an increase in the volume of the brine, which leads to a decrease in the boron content, and a high concentration (more than 20.0 wt.) - y crystallization of sodium chloride, which can negatively affect boron sorption. The optimum pH value of the method for extracting boron from these waters is 3,, 0. After the boron is removed, the brine is sent for further evaporation under natural or plant conditions, which is continued until the density reaches 1330-13 0 kg / m. At the same time, sodium chloride contained in brine is precipitated to 9295. It is separated, washed with sodium chloride solution, from shat, and released as a marketable product. The washings after triple use are added to the mother liquor and sent for further evaporation, which is carried out to a density of 1-30% 0 kg / m. At the same time, magnesium salts (CCE) and tachyhydrite (CaCB jix12H (iO)) are precipitated. They are separated and treated in the cold with initial waste water in a ratio of 1: 1, while up to 60-70 potassium chloride contained in the salt mixture remains. as a solid precipitate, which is separated, dried and discharged as a marketable product. Changing the values of these ratios reduces the yield of potassium chloride. The mother liquor after decomposition is combined with the mother liquor left after the separation of the magnesium salts, and the combined solution is treated with a caustic solution trap to a pH of 9.5-9.7 (or .NciOH 1: 1.75) to precipitate magnesium hydroxide. The precipitated magnesium hydroxide is separated and calcined to produce commercial magnesium oxide. In this case, the recovery rate of magnesium is 96-98. Less than 8, alkali increases the volume of treated water, and slows down the process of precipitation of magnesium hydroxide above 10. The increase in the pH from this limit causes precipitation of calcium and strontium hydroxide, and a decrease in it decreases the degree of extraction of magnesium from brine, which leads to degradation the resulting products. The mother liquor after separation of magnesium hydroxide is neutralized with 2.5, hydrochloric acid to pH 7.07, 5. A low concentration (below 2.5) of the acid used leads to an increase in the volume of water being processed, and a high concentration (greater than 0%) increases the content of sodium chloride in brine and releases it into the solid phase, which is undesirable for sorption npo ectoB . After the extraction of lithium and strontium by the sorption method, it is sent for further evaporation to a density of H20-1 25 kg / m. In this case, the sodium chloride contained is precipitated, which is separated, washed with sodium chloride solution, dried and discharged as a product. The mother liquor containing 39-30% calcium chloride is produced as a marketable product. Thus, the processing of wastewater iodide-bromine production allows to obtain a solution of calcium chloride, gypsum, sodium chloride, potassium chloride, magnesium oxide, as well as concentrates for the production of boron, lithium and strontium under favorable conditions for extracting the latter from the waters. e p; Waste water of iodine-bromine production, having a composition, wt.%: NaCP 9.71; CaCe, j 2.00 MgCe, 2 CaSO 0.06; CCE 0.09; Salt 12.25; B. OD 0.02; Li is 0.000 and 5g 0.030 and pH 2.6, is concentrated in the evaporator to a salt content of 20%, and it is preliminarily cleaned of mechanical impurities, acidic organic components are precipitated from it, and gypsum falls out. The clarified brine is neutralized with 20% sodium hydroxide solution to a pH of 0 and sent to the extraction of boron using ion exchange resins. The liberated brine is sent to a second evaporator where it is concentrated to a density of 1330 kg / m, with 95% of sodium chloride contained in the brine falling In: solid phase, the residue is separated, washed with sodium chloride solution and dried. The washings after three times of use are returned to the second evaporator. The mother liquor is further concentrated in a third evaporator to a density of I + jO kg / m, while carnallite and tachydrite are precipitated from it. The precipitate is separated and decomposed in cold with the initial waste water at a ratio of 1: 1, while about J0% of potassium chloride contained in the precipitate remains in the solid phase. It is separated from the solution and dried. The wash solution, containing mainly calcium and magnesium chlorides, is combined with the mother liquor and treated with a 10% sodium hydroxide solution at pH 9.6, while precipitating magnesium hydroxide. Alkali consumption is 175% of theoretical, magnesium recovery rate is 98%. Magnesium hydroxide is separated from the solution and calcined to produce magnesium oxide. After precipitation, the mother liquor (magnesium oxide hydroxide) is neutralized with 2.5% hydrochloric acid to pH. The resulting brine containing 23% of salts and having a density of 1210 kg / m is sent to the sorption method for the extraction of lithium and strontium (9). After the extraction of these components, the brine is evaporated in a fourth evaporator, where it is precipitated into the solid phase 9b of the sodium chloride contained, washed with a solution of sodium chloride and dried. Royal brine, having a density of kg / m and containing kO% calcium chloride, is produced as a marketable product. Thus, during the processing of 1 ton of waste drilling water receive, kg: gypsum 0.5; sodium chloride 99; potassium chloride 0.6; magnesium oxide 1.6; 0% calcium chloride 51 solution, as well as concentrates, with content,%: boric anhydride 0.03; lithium is 0.008 and the Q, k. For these components, an enrichment of 1.6, 13, and 12 times, respectively, is achieved and favorable conditions are created for their recovery by sorption methods. The consumption of reagents per 1 ton of waste water is, kg: caustic soda 5.9; hydrochloric acid (based on 100% HCE) 0.8; fresh water 3 kg. Technical and economic efficiency of the method consists in the possibility of complex processing of waste water with the extraction of all useful components, the elimination of the discharge of these waters and the solution of environmental problems. Claims A method for processing waste waste from iodide-bromine production, including the extraction of trace elements of magnesium hydroxide, which is characterized by the fact that, in order to extract all the useful components contained in the waste water and to create waste-free technology, the water is concentrated to 18-20% c separating the calcium sulphate formed, then treated with a 15-20% alkali solution about pH 3.5 - ", 0 with boron taken out by ion exchange, then evaporated to 1330-13 kg / m and the excreted chlorine is separated Risto sodium, and the solution

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re-evaporated to a density and lithium and strontium sorbHjO kg / m are removed with separation. melted with magnesium, after which the solution is again evaporated by carnallite and dusted to a density of 1 20 20-1 25 kg / m3, the hydrite, which is decomposed by the precipitated sodium chloride is separated, and the remaining chlorine solution with an initial waste water is equal in proportion to the calcium produced in the form of potassium chloride and the mother liquor, which is added to the solution.

the remaining magnets taken after isolation into account in the examination of zial salts, then the combined "1. Nemtsov V.G. The preparation of the complex solution is treated with 8-10% micronutrients from wastewater with an alkaline solution to a pH of 9,, 7 with fertilizer production. Dis. on the competition by dividing the precipitated magnesium hydroxide, academic, degree of candidate. tech. sciences. M, and the solution is treated with 2.5 0% 1966, p. 1b5 {All-Union Correspondence Ambulatory Acid up to pH 7.0-7.5 (Literary Institute).