[go: up one dir, main page]

WO2013066189A1 - Procédé en continu pour la concentration d'iodure - Google Patents

Procédé en continu pour la concentration d'iodure Download PDF

Info

Publication number
WO2013066189A1
WO2013066189A1 PCT/NO2012/050211 NO2012050211W WO2013066189A1 WO 2013066189 A1 WO2013066189 A1 WO 2013066189A1 NO 2012050211 W NO2012050211 W NO 2012050211W WO 2013066189 A1 WO2013066189 A1 WO 2013066189A1
Authority
WO
WIPO (PCT)
Prior art keywords
iodide
iodine
concentration
solution
amylose
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/NO2012/050211
Other languages
English (en)
Inventor
Thorstein Dyrstad
Odd Henning Sirnes
Tom Sirnes
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of WO2013066189A1 publication Critical patent/WO2013066189A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B7/00—Halogens; Halogen acids
    • C01B7/13—Iodine; Hydrogen iodide

Definitions

  • the present invention relates to a method for concentration of iodide from a first aqueous, iodidic solution and to a second aqueous, iodidic solution.
  • the concentrated aqueous, iodidic solution may be used for further production of elementary iodine. More specifically the present invention relates to using an amylose-containing material in a continuous concentration process and a method for continuous downstream processing of iodine-amylose-complex.
  • Iodine is an element that does not exist in nature in a pure condition, but in ionized condition, most often in the form of iodide ( ).
  • the metallic form of iodine (I 2 ) is called elementary iodine.
  • Iodine may also occur as iodate (I0 3 ⁇ ).
  • iodine will be used for elementary iodine, iodide and iodate, and iodic will be used to describe a solution that may contain elementary iodine, iodide or iodate.
  • saline water pumped up from wells in the ground.
  • Such wells may be gas-producing wells or oil-producing wells.
  • the water from gas-producing and oil-producing wells is also named produced water.
  • Produced water may contain hydrocarbons.
  • Such saline water may contain various amounts of iodine.
  • the salt in the salt water is substantially in the form of NaCI.
  • the saline, produced water will in the following be described as feed water.
  • the feed water will contain small amounts of iodine.
  • Commercial extraction may take place at a start concentration of iodide of 5-150 ppm, but the iodide contents are most often in the range 7-30 ppm.
  • Good sources may contain 50-70 ppm of iodide. It is known to commercially exploit salt water from the Japanese Minami Kanto gas field where the iodide contents are 100-300 ppm and from the Anakardo Basin gas field in Oklahoma, USA, where the iodide contents may be as high as 1500 ppm.
  • a known method is first to cleanse the feed water of hydrocarbons and thereafter acidify the feed water with a mineral acid, as for example sulphuric acid (H 2 S0 4 ). Iodine will then be available as HI in the acidified feed water. Thereafter an oxidizing agent as for example chorine (Cl 2 ) is added and elementary iodine is formed according to the reaction :
  • a mineral acid as for example sulphuric acid (H 2 S0 4 ).
  • This solution contains low concentrations of iodine. Concentration may be done by blowing air through the solution, possibly after heating of the solution. Iodine then will evaporate and be brought into an absorption tower. This tower is called a "blow out tower". The tower has an acidic environment and sulphur dioxide is added in order to reduce iodine to iodide:
  • Recent techniques comprise process steps where iodine in the acidified feed water is captured by ion exchange in an anion-exchange resin as described in US patent No. 3,346,331.
  • the anion-exchange resin is saturated, the anion-exchange resin is treated with a NaOH-solution followed by a NaCI-solution in order to elude iodine from the anion-exchange resin in the form of iodide and iodate.
  • Iodine in the elusion is recovered by adding mineral acid such that iodide and iodate are converted to elementary iodine which then crystallizes.
  • US patent No. 4,131,645 discloses to lead feed water directly over an anion-exchange resin without any preceding acidification and oxidation.
  • Patent specification WO 2010/056864 Al discloses to oxidize iodide by means of hypochlorite produced in situ from the chlorine contents of the produced water.
  • the produced water is preferably filtered in order to remove particles and other filterable impurities before the water is acidified.
  • Elementary iodine is captured in the subsequent step by an anion-exchange resin or by an adsorption unit comprising activated carbon. Iodine is separated from the anion-exchange resin by a NaOH- solution. Thereafter the solution is acidified to a pH between 0.5 and 3 with HCI. Then sodium-hypochlorite (NaOCI) is added in order to oxidize iodide and iodine is deposited.
  • NaOCI sodium-hypochlorite
  • Iodine is separated from activated carbon by leading sulphur dioxide gas (S0 2 ) and water therethrough.
  • the solution will contain hydrogen-iodide (HI) and sulphuric acid (H 2 S0 4 ).
  • the iodide may be oxidized by adding hydrogen-peroxide (H 2 0 2 ) and elementary iodine is deposited.
  • anion-exchange resins become ineffective as they are overgrown by hydrocarbons that may be present in the feed water.
  • the patent specification SU827376 discloses a method for extracting iodine from produced water from oil wells and ground water where the steps comprise of acidifying the iodic feed water, adding starch to the acidic feed water and letting the iodine- starch-solution sediment.
  • a flocculating agent constituting a salt of the polymer 2-methyl-5-vinylpyridin dimethyl sulfate is added.
  • the washed iodine-starch slurry is treated with acidic sulfite solution in order to isolate iodine from the starch.
  • the iodine solution which may contain 0.4-0.5% iodine, is made alkaline and is treated further in order to extract iodine in a per se known way. A continuous process is not described.
  • the patent specification FR945359 discloses a method for extracting iodine from marine algae.
  • the extract from marine algae is acidified with sulphuric acid.
  • Sodium nitrite is added to the acidic solution as an oxidizing agent.
  • Starch is added to the solution for the formation of starch-iodide.
  • the starch-iodide is deposited and clear iodine-free residual fluid is decanted.
  • the starch-iodide is brought into suspension with water and sodium-bisulfite-solution or potassium-bisulfite-solution is added as a reducing agent. After some time the iodic supernatant is decanted.
  • the deposited starch is washed and the wash water is added to the iodic supernatant.
  • the patent specification FR897641 discloses a method for extracting iodine from marine algae.
  • the extract from marine algae is acidified with sulphuric acid.
  • An oxidizing agent as for example sodium nitrite is added to the acidic solution.
  • the solution is mixed with starch or amylose-material.
  • Starch-iodide is separated from the iodine-depleted medium. Several possible methods for processing of the starch-iodide are described.
  • One method is to wash the starch-iodide with a concentrated solution of a sulfite and an alkali-hyposulfite and thereafter separate by decanting the starch material from the iodidic fluid. No continuous process is described.
  • the invention has for its object to remedy or to reduce at least one of the drawbacks of the prior art, or at least to obtain a useful alternative to prior art.
  • the present invention provides a method for extraction of an aqueous, iodidic concentrate which thereafter may be processed to elementary iodine.
  • the basis for the process is water which comes from underground, geological formations, as the water may appear alone as a fluid in the formation or comes from hydrocarbon formations.
  • the present invention relates to a continuous process for extraction of an aqueous, iodidic concentrate.
  • a continuous process is preferable compared to known processes using sedimentation, possibly also flocculation, and decanting in one or more process steps.
  • the present invention relates to a method for concentration of iodide from a first aqueous, iodidic solution and to a second aqueous, iodidic solution, the method comprising the steps:
  • step b) to add an oxidizing agent to an acidic solution from step a) in order to oxidize iodide to elementary iodine;
  • step c) to add an amylose-containing material to a solution from step b) such that an iodine-amylose-complex is formed;
  • step c) to substantially separate the iodine-amylose-complex formed in step c) from the fluid;
  • step d) to add a reducing agent to an iodine-amylose-complex fraction containing the iodine-amylose-complex from step d) in order to reduce elementary iodine to iodide to separate iodide from amylose;
  • step f) to separate a mixture from step e) into a second aqueous, iodidic solution and an amylose-containing fraction
  • step d) comprise to use a continuous operable device comprising a filter.
  • Produced water from a gas-producing well or from an oil-producing well may constitute the first iodidic solution.
  • the first iodidic solution may also come from a well which is in connection with groundwater that does not contain hydrocarbons.
  • Step f) may comprise using a continuously operable separation device comprising a filter.
  • Step b) may comprise adding an oxidizing agent chosen from a group
  • Step b) may comprise adding hydrogen peroxide (H 2 0 2 ) as an oxidizing agent.
  • Step e) may comprise adding a reducing agent chosen from a group comprising reducing sulphur-compounds, tocopherols and reducing acids.
  • the method may further comprise filtering the first iodidic solution previous to step a) in order to remove impurities from the first iodidic fluid.
  • the solution may be filtered through a continuously operable filter chosen from a group comprising continuously operable ceramic membrane filters, continuously operable ceramic ultra-membrane filters and continuously operable polymer membrane filters.
  • the filter may have a pore size from and including 0.01 ⁇ to and including 2 ⁇ .
  • the filter in step d) may be chosen from a group comprising continuously operable ceramic membrane filters, continuously operable ceramic ultra-membrane filters and continuously operable polymer membrane filters.
  • the filter may have a pore size from and including 0.01 pm to and including 2 pm.
  • the filter in step f) may be chosen from a group comprising continuously operable ceramic membrane filters, continuously operable ceramic ultra-membrane filters and continuously operable polymer membrane filters.
  • the filter may have a pore size from and including 0.01 pm to and including 2 pm.
  • Said filters may be the same type of filter in the different steps of the process, or they may be different types of filters.
  • the pore size may be the same in the different steps of the process, or it may be different and adapted to the actual step of the process.
  • step d) comprises to use a separation device that may be operated such that the concentration between iodide in the first, aqueous, iodidic solution and iodine in the iodine-amylose-complex fraction is at least 1 : 150.
  • the separation device may be operated such that the concentration between iodide in the first, aqueous, iodidic solution and iodine in the iodine-amylose-complex fraction is at least 1 : 250.
  • the separation device may be further operated such that the concentration between iodide in the first aqueous, iodidic solution and iodine in the iodine-amylose-complex fraction is at least 1 : 500.
  • the separation device may be further operated such that the concentration between iodide in the first aqueous, iodidic solution and iodine in the iodine-amylose-complex fraction is at least 1 : 750.
  • the separation device may be further operated such that the concentration between iodide in the first aqueous iodidic solution and iodine in the iodine-amylose-complex fraction is at least 1 : 1000.
  • Fig. 1 shows a flow chart for one embodiment of the invention. Step 1
  • the reference numeral 1 denotes a process according to the invention.
  • Organic components in a feed water 2 are removed by means of filtering in a filter 3.
  • Particularly feed water 2 from geological formations containing hydrocarbons could comprise organic components that may have an interruptive effect on the subsequent steps of the process.
  • a membrane filter 3 with a pore size from 0.01 pm to 2 pm is suitable for the purpose.
  • a ceramic membrane filter 3 with a pore size from 0.01 pm to 2 pm is particularly suitable for the purpose.
  • a ceramic ultra-filtering membrane filter 3 with a pore size from 0.01 pm to 0.05 pm is particularly suitable for the purpose.
  • a polymer membrane with pore size from 0.01 pm to 0.05 pm may be used in the filter 3
  • Said membrane filter 3, ceramic membrane filter 3 and ceramic ultra-filtering membrane filter 3 may be arranged for continuous operation.
  • Required negative or positive pressure relative to the ambient pressure in order to drive the feed water 2 through the filter 3 is dependent on the chosen type of filter and pore size and the person skilled in the art will know how to calculate this.
  • the retentate 34 may for example contain 1-5% hydrocarbons depending on the concentration of these in the feed water 2.
  • the retentate 34 may be led to an outlet, led back to the geological structure or be processed for extraction of the hydrocarbons. The retentate 34 will not be discussed any further herein.
  • the acidifying agent is added to the iodic permeate 32 from step 1.
  • the acidifying agent may be a mineral acid, as for example sulphuric acid (H 2 S0 4 ) or hydrochloric acid (HCI).
  • the acidifying agent is dosed to the permeate 32 by means of a per se known dosing device 4 which may comprise a first holding tank 40 for the acidifying agent, a first metering pump 41 and a pH-meter (not shown).
  • the permeate 32 may be acidified to a pH between 6.5 and 0.5.
  • step 1 may be left out.
  • the acidifying agent is in this method added to the feed water 2.
  • An oxidizing agent is added to the acidified permeate 32' from step 2A or to the acidified feed water 2'.
  • the oxidizing agent may for example be chlorine, a
  • hypochlorite compound as for example sodium-hypochlorite (NaOCI), or hydrogen-peroxide (H 2 0 2 ).
  • the oxidizing agent is dosed to the acidified permeate 32' or the acidified feed water 2' by means of a per se known dosing device 4 which may comprise a second holding tank 42 for the oxidizing agent and a second metering pump 43. It is skillful to choose a proper concentration for the oxidizing agent based on the desired volume ratio between acidic permeate 32' or acidic feed water 2', and oxidizing agent, and how the acidic permeate 32' or the acidic feed water 2' and the acidifying agent are to be mixed. Iodide in the acidic permeate 32' or in the acidic feed water 2' will oxidize to elementary iodine in and after step 2B.
  • amylose-containing fluid is added to the permeate 32" or to the feed water 2" from step 2B.
  • the amylose-containing fluid may for example be an aqueous starch solution.
  • the starch may be added to the permeate 32" or the feed water 2" from step 2B in dry condition and suspended in the permeate 32" or the feed water 2".
  • Known starches have different ratios between amylopectin and amylose.
  • Amylose may make up from 20% to 30% of the total amount of starch. By breeding or genetic modification of plants, this ratio may be changed such that the amylose-portion of the starch increases beyond 30% in the plant's starch-containing organ or organs.
  • the amylose-containing fluid is dosed to the permeate 32" or the feed water 2" by means of a per se known dosing device 4 which may comprise a third holding tank 44 for the amylose-containing fluid and a third metering pump 45. It is skillful to choose a proper concentration for the amylose-containing fluid based on the desired volume ratio between permeate 32" or feed water 2", and amylose-containing fluid, and how the permeate 32" or the feed water 2" from step 2B and the amylose-containing fluid are to be mixed.
  • the temperature of the fluid may be held lower than 55 °C in the third holding tank 44. If necessary the temperature in the permeate 32" or the feed water 2" is reduced to less than 55 °C before the permeate 32" or the feed water 2" is mixed with the amylose- containing fluid or alternatively with the dry starch. This may be done in a per se known way in for example a countercurrent plate heat exchanger (not shown) and is not discussed any further herein.
  • the temperature in the feed water 2 may be adjusted prior to the membrane filter 3 of step 1, just after the membrane filter 3 in step 1, just after step 2A or just after step 2B.
  • the mixture of permeate 32" or feed water 2" and the amylose-containing fluid is mixed further in a proper, first mixing apparatus 50.
  • a mixing apparatus 50 of the flow-through type is suitable for this purpose, for example a static mixer of per se known type.
  • the mixture 36 of permeate 32" or feed water 2" and the amylose-containing fluid from step 2C is led to a reaction tank 60 in order for iodine in the mixture 36 to have time to form complex with the amylose.
  • the iodine-amylose-complex is coloured bluish-black to black.
  • the detention time of the mixture 36 in the reaction tank 60 is decided based on the amount of iodine in the feed water 2 and the concentration of amylose in the amylose-containing fluid, among other things.
  • the reaction tank 60 may be arranged to batch-fill and batch-tap. In an alternative embodiment the reaction tank 60 may be arranged for continuously filling and tapping .
  • a first separation device 70 arranged to be able to separate the iodine-amylose-complex from the essential of the fluid .
  • a first separation device 70 may comprise a filter.
  • the filter 70 may comprise a ceramic membrane filter.
  • the ceramic membrane filter 70 may comprise a ceramic ultra-membrane filter.
  • the filter 70 may comprise a polymer membrane filter, or it may comprise a combination of two or more filters 70.
  • the filter 70 may be a membrane filter with a pore size from and including 0.01 pm to and including 2 pm.
  • the filter 70 may be arranged for continuous operation.
  • a concentrated iodine-amylose-complex fraction 80 and a separated fluid 82 comprising any excess iodine and other dissolved matters as for example salts and saccharides.
  • the separated fluid 82 may be led to outlet and will not be discussed any further herein. It is essential to the invention that the separation device 70 is chosen in such a way or is operated in such a way that the material flow containing the iodine-amylose fraction 80, constitute a slurry or at least shows a pumpable consistency.
  • the separation device 70 may be operated such that the concentration between iodide in the feed water 2 and iodine in the iodine-amylose-complex fraction 80 is at least 1 : 150.
  • the separation device 70 may be operated such that the concentration between iodide in the feed water 2 and iodine in the iodine-amylose-complex fraction 80 is at least 1 : 250.
  • the separation device 70 may be fu rther operated such that the concentration between iodide in the feed water 2 and iodine in the iodine-amylose-complex fraction 80 is at least 1 : 500.
  • the separation device 70 may be operated such that the concentration between iodide in the feed water 2 and iodine in the iodine-amylose- complex fraction 80 is at least 1 : 750.
  • the separation device 70 may be operated such that the concentration between iodide in the feed water 2 and iodine in the iodine- amylose-complex fraction 80 is at least 1 : 1000.
  • the iodine-amylose-complex fraction 80 from step 3 is possibly added water to a proper consistency in a per se known way (not shown), for example such that the ratio between the iodine-amylose-complex fraction 80 and added water is 1 : 1.
  • a reducing agent is dosed to the aqueous iodine-amylose-complex fraction 80 by means of per se known dosing device 4 which may comprise a fourth holding tank 46 for the reducing agent and a fourth metering pump 47. It is skillful to choose a proper concentration for the reducing agent based on the desired volume ratio between aqueous iodine-amylose-complex 80 and reducing agent, and how iodine- amylose-complex 80 and the reducing agent are to be mixed .
  • the reducing agent may for example be a reducing sulphur compound, a tocopherol or a reducing acid.
  • the reducing sulphur compound may for example comprise thiosulphate (S 2 0 2 2- ).
  • the reducing sulphur compound may comprise a sulfite, where the sulfite may comprise for example bisulfite (HS0 3 " ) such as for example sodium bisulfite (NaHS0 3 ) or metasulfite (S 2 0 5 ⁇ ), such as for example sodium metasulfite (Na 2 S 2 0 5 ), also known as sodium pyrosuifite.
  • the reducing acid may for example be ascorbic acid (C 6 H 8 0 6 ) or oxalic acid (H 2 C 2 0 4 ).
  • Iodine quickly reduces to iodide and separates from the amylose on adding of the reducing agent.
  • the mixture 80' of iodine-amylose-complex fraction 80 and the reducing agent may be led through a second mixing apparatus 52 as for example a static mixer of per se known type.
  • the mixture 80' of amylose and separated iodide from step 4 is brought to a second separation device 72 arranged to be able to separate amylose from the iodic fluid.
  • a second separation device 72 may comprise a filter.
  • the filter 72 may comprise a ceramic membrane filter.
  • the ceramic membrane filter may comprise a polymer membrane filter, or it may comprise a combination of two or more filters 72.
  • the filter 72 may be a membrane filter with a pore size from and including 0.01 pm to and including. 2 pm.
  • the filter 72 may be arranged for continuous operation.
  • the separation device 72 is chosen or operated such that the material flow containing the amylose-containing fluid 90, constitutes a slurry or at least shows a pumpable consistency.
  • the second aqueous, iodidic solution 92 may in addition to iodide also contain residues of the reducing agent.
  • the second aqueous, iodidic solution 92 is a concentrate of iodide and contains substantially more iodide than the feed water 2 per unit of space.
  • the second aqueous, iodide concentrate 92 may be further treated on-site with per se known techniques, as for example the "blow out" method, to produce elementary iodine, or the second aqueous, iodide concentrate 92 may be transported to another location for further processing.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de concentration d'iodure à partir d'une première solution aqueuse d'iode (2) et une seconde solution aqueuse d'iode (92). Le procédé comprend les étapes : a) acidifier la première solution (2 ; 32) par un acide minéral ; b) ajouter un agent oxydant à une solution acide (2' ; 32') provenant de l'étape a) de façon à oxyder l'iodure en iode élémentaire ; c) ajouter une matière à teneur en amylose à une solution (2'' ; 32'') provenant de l'étape b) de telle sorte qu'un complexe iode-amylose soit formé ; d) séparer de façon substantielle le complexe iode-amylose formé à l'étape c) à partir d'un fluide (36) ; e) ajouter un agent réducteur à une fraction du complexe iode-amylose (80) contenant le complexe iode-amylose provenant de l'étape d) de façon à réduire l'iode élémentaire en iodure de façon à séparer l'iodure de l'amylose ; et f) séparer le mélange (80') provenant de l'étape e) en une seconde fraction aqueuse d'iode (92) et une fraction à teneur en amylose (90), où l'étape d) comprend l'utilisation d'au moins un dispositif de séparation (70) comprenant un filtre.
PCT/NO2012/050211 2011-10-31 2012-10-30 Procédé en continu pour la concentration d'iodure Ceased WO2013066189A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
NO20111476 2011-10-31
NO20111476 2011-10-31
US201161556342P 2011-11-07 2011-11-07
US61/556,342 2011-11-07

Publications (1)

Publication Number Publication Date
WO2013066189A1 true WO2013066189A1 (fr) 2013-05-10

Family

ID=48192422

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/NO2012/050211 Ceased WO2013066189A1 (fr) 2011-10-31 2012-10-30 Procédé en continu pour la concentration d'iodure

Country Status (2)

Country Link
NO (1) NO336304B1 (fr)
WO (1) WO2013066189A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112194204A (zh) * 2020-09-10 2021-01-08 昆明铂锐金属材料有限公司 一种高纯三碘化铑的制备方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR897641A (fr) * 1943-04-22 1945-03-27 Bretonne De Prod Chim Et Pharm Perfectionnement à la préparation de l'iode, notamment à son extraction et à celle de l'algine à partir des végétaux marins
FR945359A (fr) * 1947-04-02 1949-05-03 Procédé d'extraction de l'iode des jus de lessivage des algues marines
US3346331A (en) * 1964-05-04 1967-10-10 Rohm & Haas Recovery of iodine from solutions containing same
SU827376A1 (ru) * 1979-07-12 1981-05-07 Предприятие П/Я Р-6767 Способ извлечени иода
WO2010033945A1 (fr) * 2008-09-19 2010-03-25 Arysta Lifescience North America, Llc Systèmes et procédés de récupération d’iode
WO2010056864A1 (fr) * 2008-11-12 2010-05-20 Becker Thomas M Système de récupération d’iode

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR897641A (fr) * 1943-04-22 1945-03-27 Bretonne De Prod Chim Et Pharm Perfectionnement à la préparation de l'iode, notamment à son extraction et à celle de l'algine à partir des végétaux marins
FR945359A (fr) * 1947-04-02 1949-05-03 Procédé d'extraction de l'iode des jus de lessivage des algues marines
US3346331A (en) * 1964-05-04 1967-10-10 Rohm & Haas Recovery of iodine from solutions containing same
SU827376A1 (ru) * 1979-07-12 1981-05-07 Предприятие П/Я Р-6767 Способ извлечени иода
WO2010033945A1 (fr) * 2008-09-19 2010-03-25 Arysta Lifescience North America, Llc Systèmes et procédés de récupération d’iode
WO2010056864A1 (fr) * 2008-11-12 2010-05-20 Becker Thomas M Système de récupération d’iode

Also Published As

Publication number Publication date
NO336304B1 (no) 2015-07-27
NO20121266A1 (no) 2013-05-01

Similar Documents

Publication Publication Date Title
KR102298822B1 (ko) 수질 정화를 위한 염소화 보조 응고 방법
JP5648871B2 (ja) 炭酸ガスの処理方法
JP6279295B2 (ja) 超純水製造システム及び超純水製造方法
US20100119438A1 (en) Iodine recovery system
NO338600B1 (no) Fremgangsmåte for utvinning av hydrokarboner ved injisering av behandlet vann med lav saltholdighet inn i en hydrokarbon¬bærende formasjon
US8591743B2 (en) Portable system for on-site iodine extraction from an aqueous solution
EP3058119A1 (fr) Processus d'extraction de saumure
JP2010082526A (ja) 炭酸ガスの処理方法
CA2869302C (fr) Systeme et methode de traitement d'eau
CN106995245A (zh) 借助加药装置和延长螯合树脂塔运行时间深度去除盐水中杂质的方法
WO2013066189A1 (fr) Procédé en continu pour la concentration d'iodure
US8303163B2 (en) In-line mixing apparatus for iodine extraction
JP5678436B2 (ja) 超純水製造方法及び装置
CN206447713U (zh) 全膜法海水淡化及浓盐水综合利用系统
JP2005187306A (ja) 油田かん水からのヨウ素製造方法
Bhatkar et al. Modifications of petroleum industry effluent treatment Method: An approach for quality improvement of process water for ASP flooding and chemical EOR
WO2013026068A1 (fr) Procédé de récupération continue de dioxyde de carbone à partir d'eau de mer acidifiée
JP2008237986A (ja) ホウ素含有水の処理方法
CN214400104U (zh) 一种edi浓水回收再利用系统
US20140091040A1 (en) Bicarbonate conversion assisted ro treatment system for natural gas flowback water
US20250320581A1 (en) Filtering brine streams from direct lithium extraction units using flow rates adjusted based on electrical conductivity
CN110577309A (zh) 一种压裂返排液处理系统及工艺
NO332199B1 (no) Metode og apparat for samtidig gjenvinning av energi og rensing av vann.
CN102557158B (zh) 煤层气田产出水的处理方法
CN104229856B (zh) 一种利用废水脱盐兼制备轻质硫酸钡的方法及其装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 12846689

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 12846689

Country of ref document: EP

Kind code of ref document: A1