[en] The chelation of metals ion (Cu²⁺, Cd²⁺ and Cr³⁺) with processyields of humic acid from peat soil has been done. The chelatizationcalculation was carried out using a mathematical model of the metals ionneutralization to the humic acid functional group. The model has superioritydue to the introduction of the humic acid concentration conditional and theloading capacity. Chelation is expected to obtain the constant experimentthat agrees with environmental conditional were the chelatization to takeplaces. By the tree neck flask of bath reactor, 250 ml volume at thetemperature of 25 ^oC chelation have been done and the AAS was used toanalyzes the yield. By mathematical calculate was obviously proved that thechelation constants was not influenced by pH, ionic strength and origin peatsoils. As log β, chelation constants of Cu²⁺, Cd²⁺ and Cr³⁺ were4.67 (± 0.02); 5.98 (± 0.02) and 6.09 (± 0.01) for humic acid fromSumatra I (Silaut III) and 4.68 (± 0.01); 5.97 (± 0.02) and 6.09 (±0.02) for Sumatra II (Silaut IV). While chelation constant Cu²⁺, Cd²⁺ andCr³⁺ from Kalimantan were 4.66 (± 0.03); 5.99 (± 0.01); 6.08 (±0.02). (author)

[en] Extraction yttrium from xenotime concentrate has been done. Feed of extraction was rare earth xenotime concentrate (Yttria group) have been separated from ceria group. Stripping process of extract phase used nitric acid and sulphuric acid. Determination of yttrium (Y), and impurities of rare earths other was as lanthanum (La), cerium (Ce), and neodymium (Nd) was analyzed by spectrometer X-ray. The purposed of this research was obtained separated yttrium relative pure. At process of extraction variable influence were concentration of nitric acid in feed, time of extraction, and concentration of extractant in organic phase. At process of stripping variable influence were kind of acid and concentration of acid. At this research optimum condition of extraction process was molarity of nitric acid = 1 M, time of extraction = 15 minutes, and concentration of extractant = 30% organo phosphor D₂EHPA in dodecane. At that optimum condition was found extraction efficiency of yttrium = 98.03%, with impurities of La = 198 ppm, Ce = 213 ppm, and Nd = 132 ppm. At stripping process was the best acid used sulphuric acid was 8 M and time of stripping was 29 minutes. At this condition was found efficiency of stripping = 79.29%, with impurities of La = 85 ppm, Ce = 36 ppm, and Nd = 25 ppm. (author)

[en] The effective of zeolite and humic substance as adsorbent on adsorptionof Sr and Zr has been done. The absorption process was done by addedadsorbent into 10 ml solution of Sr 1000 ppm and 10 ml solution of Zr 1000ppm followed by agitation. After reached the equilibrium condition and thenwas separated its solid from filtrate. The content of Sr and Zr on adsorbentware determined by analysis of filtrate by using X ray fluorescent. Theparameters studied ware the influence of weight adsorbent added and time ofagitation versus adsorption of Sr and Zr. The result of the experimental wereaddition of 50 mg zeolite into 10 ml solution of Zr of 1000 ppm and Sr of1000 ppm has the efficiency of adsorption of Zr = 94.20% and efficiency ofadsorption of Sr = 27.50% with time of agitation = 120 minutes. Theexperiment using humic substance has efficiency of adsorption of Zr = 64.20%and efficiency of adsorption of Sr = 55.60%. So the adsorption of Zr wasbetter using zeolite as adsorbent. The adsorption of Sr was better usinghumic substance as adsorbent. (author)

[en] The existence of zircon (ZrSiO_4) in the nature is mostly associated with some of the valuable oxide compounds (VOC), such as TiO_2 and rare earth oxides (REO). The existence of natural minerals in Indonesia containing zirconium (Zr) and REO lies in 13 regions, ranging from Aceh to West Papua province. Based on those aforementioned aspects, the goal of this research is to conduct the study of integrated technology of local zircon sand processing containing TiO_2 and REO. The study was conducted by analyzing the content of VOC in zircon sand samples from the areas of Landak and Tumbang Titi West Kalimantan and Bangka by using XRF. Based on the content of VOC in this zircon sand, it can be predicted that the zircon sand from the area of Landak and Tumbang Titi West Kalimantan and Bangka contains mineral zircon (ZrSiO_4), ilmenite (FeTiO_3), monazite (LREE, Th)PO_4, and xenotime (HREE, Th)PO_4. Based on these types of mineral, the flow chart of beneficiation technology process to increase the concentration of each mineral and the flow chart of zircon concentrate process into ZrO_2(zirconia) and ZrOCl_2.8H_2O (zirconium oxychloride) industrial grade and zirconia and zirconium chemicals nuclear grade, ilmenite into TiO_2, monazite into Nd_2O_3, and Th(OH)_4 concentrate, xenotime into Y_2O_3, Gd_2O_3, and Th(OH)_4 concentrate are obtained in one area of pilot plant or an integrated factory. The results of the study concluded that the concept of local processing of zircon sands containing monazite, xenotime, and ilmenite can be either integrated in the region with the results of multi-product plant. If it can be realized in Indonesia with the addition of an integrated waste water treatment system, then in addition to safe for the environment can also save on production costs and give economic added value for shareholders zircon mining permit. (author)

[en] Treatment process of water of free mineral and study area of processing of sea water to meet the need of water cooling of PWR. Desalination is a separation process used to reduce the dissolved salt content of saline water. All desalination processes involve three liquid streams: the saline feedwater (brackish water or seawater), low salinity product water, and very saline concentrate. Seawater Muria Jepara is feed type 1 with content salt is low and relative suspension and weight metals is low. There are two types of membrane process used for desalination: reverse osmosis (RO) and electrodialysis (ED). The starting of process is difficult and expensive. However, starting since 1950, desalination process appear to be economically practical for ordinary use. There are 3 key elements significantly affect to the technical performance and long term characteristic type, i.e. 1) energy, 2) corrosivity of seawater, and 3) desalination process technology. These elements closely inter related and important for design improvements and technical performance optimization. From the analysis of sea water of gulf Muria Jepara was found as follows : Fe = 0.176 ± 0.012 ppm, Pb = 0.612 ± 0.017 ppm, Cd = 52.567 ± 0.750 ppm, Cu = 0.044 ± 0.005 ppm, Zn = 0.061 ± 0.003 ppm, Mn = 0.057 ± 0.003 ppm, Ca between = 365.256 - 368.654 ppm, Na between = 9572.000 - 9775.000 ppm, Mg between 759.000 - 779.00 ppm and Ni = 0.524 ± 0.005 ppm. Cost production of process using reverse osmosis as around 0.9 - 1 US$/m3, while using electrodialysis is around 1.2 US$/m3, and by using evaporation process or distillation process is around 1.4 - 1.6 US$/m3. (author)

[en] Separation of uranium and ruthenium mixture in a nitric acid solution using liquid surfactant membrane consisting of the Span 80 as surfactant, mixture of di-(2-ethyl hexyl) phosphoric acid (D2EHPA) in kerosene as extractant and phosphoric acid as internal phase had been done. This technique is the combination of extraction and stripping processes designed to working simultaneously. The parameters studied included the molarity of phosphoric acid (H₃PO₄) as the internal phase, the molarity of nitric acid (HNO₃) in the feed, concentration of di-(2-ethyl hexyl) phosphoric acid in kerosene as extractant, and time of extraction. the result for the experimental separation of 20,000 ppm of uranium in 500 ppm of ruthenium mixture showed that total recovery efficiency for uranium was 87.62% at the optimum conditions, i.e. 1.5 M molarity of H₃PO₄ 3 M of HNO₃, 1 % of D2EHPA in kerosene, and 10 minutes extraction time. at such conditions a 100% uranium can be separated from ruthenium

[en] The purification of yttrium by extraction process in the solution of nitric acid rare earth with di-(2-ethylhexyl)-phosphoric acid (HDEHP) have been investigated. Feed as nitric acid rare earth solution was prepared by method digestion of xenotime sand. The contents of yttrium (Y), lanthanum (La), and cerium (Ce) rare earth were analyzed using X-ray fluorescence. The purification was done by liquid-liquid extraction process from the feed mixture of rare earth. Variable that effect the distribution of rare earth as function of concentration of nitric acid in the aqueous phase, the concentration of organic phase in kerosene, and time of extraction. The best results at the separation was obtained as follows : concentration of nitric acid = 0.5 M, the concentration of organic phase = 30% di-(2-ethylhexyl)-phosphoric acid in kerosene, and time of extraction = 15 minutes. At this condition were the value of the separation factor of Y-La 126.9403 and separation factor of Y-Ce = 89.7923. (author)

[en] Xenotime sand is one of potential natural resources, because it contains rare earth elements (REEs) among of which are Y, Dy, Gd, La, Ce, Nd that have been used a lot in various of fields both nuclear and non-nuclear. In spite of containing REEs, xenotime is also containing U and Th radioactive elements. Therefore that sand has a very strategical and economical values. This investigation aims at gaining the separation and the purification of yttrium (Y) which is relatively pure from REEs concentrate of xenotime sand processed product. The yttrium is used for developing the newer and renewable energies among of which are: yttrium aluminium garnet laser (YAG-laser), oxygen sensor solid electrolyte based Yttria-stabilized zirconia (YSZ), and solid oxide fuel cell (SOFC). The processing stages done namely xenotime sand digestion by sulfuric acid, quenching, precipitation, drying, dilution, extraction and stripping processes. The extraction processes used D2EHPA extractant which was diluted by dodecane. The stripping process used feed of extraction product (extract) with sulfuric acid. The determination of yttrium (Y) concentration, and impurities of another rare earth elements: such as dysprosium (Dy), gadolinium (Gd), lanthanum (La), cerium (Ce), neodymium (Nd), were analyzed by using X-ray fluorescence. In the yttrium (Y) extraction process, the influencing variables were: nitrate acid concentration in feed solution, D2EHPA concentration in dodecane, and extraction time. In the stripping process, the influencing variables were: sulfuric acid concentration and extraction time. From the investigated variables namely: nitrate acid molarity 1 M, extractant concentration of 30 % D2EHPA in dodecane, and extraction time of 15 minutes. In that condition yielded the extraction efficiency of Y was 98.63 %. In the stripping process, the optimum product used sulfuric acid of 4 M molarity and stripping time of 20 minutes. In this condition the stripping efficiency obtained was 59.29 %, with the impurities of Dy 198 ppm and Gd, Ce, La, Nd below 100 ppm. (author)

[en] The separation of uranium and yttrium in hydrochloric acid was extracted by D₂EHPA in dodecane. This process used liquid-liquid extraction method. The variables studied were the concentration of hydrochloric acid, the concentration of extractant, time of extraction, and the temperature of extraction. The data evaluation of the research showed that the optimum condition was as follows: the concentration of HCI = 0.2 M, the concentration of extractant = 0.15 M D₂EHPA, the time of extraction = 15 minutes, and the temperature of extraction = 20^oC. It was found that the distribution coefficient of uranium was = 34.43, the distribution coefficient of yttrium was = 2.20, and the separation factor of U-Y= 15.65

[en] Extraction of La and Nd concentrate product of monazite sand treatment byD2EHPA have done. The mayor element contained in monazite sand were Ce, Laand Nd. After separation of Ce, was obtained La and Nd concentrate. Theextraction process using D2EHPA to separate La and Nd. The extraction feed oraqueous phase was La and Nd concentrate in HNO₃. The parameter influencewere time and rate of agitation, acidity of feed and concentration of D2EHPAin kerosene. The best yield was obtained at extraction of 10 ml of feed inHNO₃ 0.2M, was extracted by 10 ml of D2EHPA in kerosene along 10 minuteswith the rate of agitation was 400 rpm. At this condition was obtaineddistribution coefficient (Kd) of La =10.34, Kd Ce =0.58, Kd Nd = 0.24 andseparation factor of (FS) La-Ce 27.21, FS of La-Nd = 43.08 and FS of Ce-Nd2.42. (author)