• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Procedure for obtaining magnesium hydroxide from saline effluents. The present invention relates to a process for obtaining magnesium hydroxide from saline effluents comprising an acidification and desorption stage for the elimination of the carbonic species and alkalization and basification stages in order to precipitate the magnesium hydroxide. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2641269A1
    申请号:ES201630410
    申请日:2016-04-05
    公开日:2017-11-08
    发明作者:Hicham EL BAKOURI；Abel RIAZA FRUTOS；José MORILLO AGUADO；José USERO GARCÍA
    申请人:Abengoa Water SL；
    IPC主号:
    专利说明:

    image 1
    image2
    image3
    image4
    image5
    image6
    image7


    Parameters Value
    Conductivity (mS / cm) 73
    pH 7.9
    Dissolved solids (mg / L) 54.6
    Calcium (mgCa2 + / L) 960
    Magnesium (mgMg2 + / L) 2.1
    Sodium (mgNa + / L) 15.3
    Chlorides (mgCl- / L) 28.7
    Sulfates (mgSO4 2- / L) 4.6
    Lithium (mgLi / L) 0.6
    Potassium (mg / L) 720
    Carbonates (mgCO3Ca / L) n.d.
    Alkalinity (mgCO3Ca / L) 445
    Table 1. Composition of residual effluent from seawater desalination plant.
    The first stage of the process consisted in the removal of calcium from the effluent by means of a
    5 carbonation process. To this end, a dose of Na2CO3 of 2 kg / m3 of treated effluent was added, a reaction time of 15 minutes was maintained and at a later stage of decantation the solid phase was separated. The analysis of the treated effluent revealed the removal of 90% of calcium, without significantly affecting the magnesium content of the brine (see table 2). Trials were also carried out by adjusting the pH at the stage of
    10 reaction with NaOH or Ca (OH) 2, obtaining good results in relation to the elimination of calcium (see tables 3 and 4).
    Na2CO3 (kg / m3) added NaOH (kg / m) addedfinal pHCa (kg / m3) final% Ca removedMg (kg / m3) final% Mg removed
    2.0 0.08.69889.820001.5
    Table 2. Effluent treated with Na2CO3.
    9


    Na2CO3 (kg / m3) added NaOH (kg / m) addedfinal pHCa (kg / m3) final% Ca removedMg (kg / m3) final% Mg removed
    2.5 809.030.996.819892.0
    3.0 409.024.797.420220.4
    Table 3. Treatment at pH 9 with NaOH.
    Na2CO3 (kg / m3) added Ca (OH) 2 (kg / m3) addedfinal pHCa (kg / m3) final% Ca removedMg (kg / m3) final% Mg removed
    2.5 3679.533.296.520041.3
    3.0 3679.627.997.119892.0
    3.5 3679.614.598.520031.3
    Table 4. Treatment at pH 9.5 with Ca (OH) 2 and Na2CO3
    5 Next, the treated effluent was transferred to a reactor to acidify it to pH 3.5 with inorganic acids (0.36 kg of H2SO4 or 0.22 kg of HCl was needed to acidify each m3 of effluent). Subsequently, a stripping was performed with air to recover the CO2, this gaseous stream was led to an absorption tower in which it was contacted in countercurrent with a NaOH stream, obtaining a solution close to
    10 saturation of Na2CO3 (200 g / L). In this way, the Na2CO3 that is recirculated to the reactor of stage a1) of carbonation is recovered, thus having an environmentally friendly process in relation to CO2 emissions.
    The acidified brine stream was transported to a downflow filter type bed
    15 formed by particles of calcined dolomite with a grain size of 20 mm. The process was developed by gravity with a speed of 50 L / min / m2 to achieve an optimal residence time and that the effluent pH was between 9.0 and 10.0.
    The resulting effluent was transported to the bizone reactor in which calcined dolomite 20 was added in the form of a slurry by adjusting the pH in a range between 11.0 and 11.5.
    The bizone reactor supernatant was transported to the bizone flocculator with a residence time of another 15 minutes. The bottom of the reactor and the flocculator are purged to prevent impurities from accumulating in both. 30% of the purge current of the bizone reactor and 25% of the bizone flocculator is returned to the reactor thus improving the reaction process and the
    10
    image8
    image9
    权利要求:
    Claims (1)
    [1]
    image 1
    image2
    image3
    类似技术:
    公开号 | 公开日 | 专利标题
    US8961916B1|2015-02-24|Methods to control flue gas and inorganics precipitation
    AU2014352663B2|2017-12-07|Systems and methods for removing minerals from a brine using electrodialysis
    US20130193074A1|2013-08-01|Water treatment process
    WO2006031732A3|2006-09-28|Water desalination process and apparatus
    US20190359512A1|2019-11-28|System for removing minerals from a brine
    SG186287A1|2013-01-30|Seawater desalination plant and production of high purity salt
    CN104071808A|2014-10-01|Method for preparing industrial salt through separation, evaporation and crystallization of coal chemical strong brine
    EA019279B1|2014-02-28|Method for purifying lithium bicarbonate
    PH12014502157A1|2014-12-10|Method for producing high-purity nickel sulfate
    US9259703B2|2016-02-16|System for removing selenium from a feed stream
    GB201203780D0|2012-04-18|Water mineralization
    ES2641269A1|2017-11-08|Procedure for obtaining magnesium hydroxide from saline effluents |
    RU2011137433A|2013-03-20|PRODUCTION OF PURIFIED CALCIUM CHLORIDE
    US9737827B2|2017-08-22|System for removing high purity salt from a brine
    JP2011162404A|2011-08-25|Method for producing sodium carbonate
    US8591852B2|2013-11-26|Method of producing soda ash and calcium chloride
    US20130216467A1|2013-08-22|Method of producing soda ash and calcium chloride
    EA201992445A1|2020-04-06|METHOD FOR PRODUCING LITHIUM CONCENTRATE FROM LITHIUM-BEARING NATURAL BRINS AND ITS PROCESSING IN LITHIUM CHLORIDE OR LITHIUM CARBONATE
    US20210188671A1|2021-06-24|Buffer-free process cycle for co2 sequestration and carbonate production from brine waste streams with high salinity
    CA2903122C|2017-05-30|Process for treating brine recovered from a coal seam gas operation
    US10843946B2|2020-11-24|Process for removing silica from produced water and other wastewater streams
    WO2012155223A8|2014-04-03|System for producing precipitated calcium carbonate from calcium carbonate slurry waste; method for calcium carbonate slurry waste recovery, processing and purification and the calcium carbonate product thereof
    ES2641852T3|2017-11-14|Procedure to recover water, metal and organic products from the production of polycarboxylic acid
    AU2011202102B2|2013-05-02|Processing of Coal Seam Gas | Water
    BR112018001304B1|2021-11-03|EFFLUENT TREATMENT PROCESS - PH REFINING FOR SULFATE REMOVAL
    同族专利:
    公开号 | 公开日
    WO2017174839A1|2017-10-12|
    ES2641269B1|2018-09-06|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2595314A|1948-10-19|1952-05-06|Kaiser Aluminium Chem Corp|Process for producing magnesium hydroxide|
    DE2450259B2|1974-10-23|1979-03-29|Bayer Ag, 5090 Leverkusen|Process for cleaning electrolysis brine|
    WO2010027247A1|2008-09-05|2010-03-11|Servicios Industriales Peñoles, S.A. De C.V.|Process for the production of high-purity magnesium hydroxide|
    法律状态:
    2018-09-06| FG2A| Definitive protection|Ref document number: 2641269 Country of ref document: ES Kind code of ref document: B1 Effective date: 20180906 |
    优先权:
    申请号 | 申请日 | 专利标题
    ES201630410A|ES2641269B1|2016-04-05|2016-04-05|Procedure for obtaining magnesium hydroxide from saline effluents|ES201630410A| ES2641269B1|2016-04-05|2016-04-05|Procedure for obtaining magnesium hydroxide from saline effluents|
    PCT/ES2017/070095| WO2017174839A1|2016-04-05|2017-02-22|Method for obtaining magnesium hydroxide from saline effluent|
    [返回顶部]