WO2010057261A1 - Utilisation de déchets de dessalement - Google Patents

Utilisation de déchets de dessalement Download PDF

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Publication number
WO2010057261A1
WO2010057261A1 PCT/AU2009/001512 AU2009001512W WO2010057261A1 WO 2010057261 A1 WO2010057261 A1 WO 2010057261A1 AU 2009001512 W AU2009001512 W AU 2009001512W WO 2010057261 A1 WO2010057261 A1 WO 2010057261A1
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WO
WIPO (PCT)
Prior art keywords
ammonia
process according
brine waste
reaction
waste
Prior art date
Application number
PCT/AU2009/001512
Other languages
English (en)
Inventor
Linda Yuan Zou
Original Assignee
University Of South Australia
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
Priority claimed from AU2008906021A external-priority patent/AU2008906021A0/en
Application filed by University Of South Australia filed Critical University Of South Australia
Priority to JP2011536704A priority Critical patent/JP2012509237A/ja
Priority to ES09827050.7T priority patent/ES2553969T3/es
Priority to EP09827050.7A priority patent/EP2361224B1/fr
Priority to CA2744264A priority patent/CA2744264A1/fr
Priority to CN2009801544359A priority patent/CN102282106B/zh
Priority to AU2009317875A priority patent/AU2009317875B2/en
Priority to US13/130,423 priority patent/US8741249B2/en
Publication of WO2010057261A1 publication Critical patent/WO2010057261A1/fr
Priority to IL213005A priority patent/IL213005A/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/16—Halides of ammonium
    • C01C1/164—Ammonium chloride
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/12—Preparation of carbonates from bicarbonates or bicarbonate-containing product
    • C01D7/123—Preparation of carbonates from bicarbonates or bicarbonate-containing product by thermal decomposition of solids in the absence of a liquid medium

Definitions

  • the present invention relates generally to processes for the production of value added materials utilising saline waste streams, such as those from desalination processes. More specifically, the present invention relates to processes for the production of soda ash (sodium carbonate, Na 2 CO 3 ) utilising saline waste streams and, optionally, carbon dioxide (CO 2 ) waste gases from combustion sources.
  • soda ash sodium carbonate, Na 2 CO 3
  • CO 2 carbon dioxide
  • RO membranes are used in desalination plants to desalinate sea water, brackish ground water and/or saline industrial waste water.
  • the main objective of the desalination process is to reduce the salt (sodium chloride, NaCI) concentration of saline water to less than 0.5 grams per litre (g/L) suitable for drinking water.
  • the salt concentration of sea water is typically 35-45 g/L.
  • one of the by-products of the desalination process is brine waste which typically has a salt concentration of about 70 g/L.
  • the highly saline liquid brine waste stream has to be disposed of and the typical methods used to do that include discharging it back to the ocean, disposing of it in the sewer, injecting it into deep wells, applying it to land, or transferring it to evaporation ponds. In each case, disposal of the waste imposes significant economic and/or environmental costs.
  • brine waste from desalination processes would be used to form other, value added materials.
  • the present invention arises from the discovery that brine waste and, optionally, carbon dioxide waste gases from combustion sources, can be used as starting materials in a process for the production of soda ash.
  • the present invention provides a process for producing soda ash from brine waste, the process including reacting brine waste with carbon dioxide and ammonia to produce soda ash, wherein at least a portion of the ammonia is regenerated from ammonium chloride produced during the reaction.
  • the process will include collecting sodium bicarbonate produced during the reaction and heating the collected sodium bicarbonate to produce the soda ash.
  • the ammonium chloride produced during the reaction will preferably be treated with a base anion exchange resin (such as a weak base anion exchange resin) to regenerate the ammonia. This regeneration will preferably occur after further treatment (such as concentrating) of the ammonium chloride produced during the reaction.
  • a base anion exchange resin such as a weak base anion exchange resin
  • the term 'brine waste' refers to a saline solution having a sodium chloride concentration of between about 50 g/L and about 250 g/L, inclusive.
  • the brine waste may be a waste stream from a desalination plant, such as a reverse osmosis desalination plant.
  • the process may also include treating the brine waste to remove at least some of any undesired inorganic cations (such as calcium, magnesium and strontium ions) present in the brine waste prior to the reaction with carbon dioxide and ammonia.
  • the undesired inorganic cations present in the brine waste may be removed either partially or entirely by selectively binding those ions with a binding agent, such as a cation exchange resin.
  • the carbon dioxide used in the process of the present invention will preferably be obtained from a waste gas stream derived directly or indirectly from combustion sources, such as coal or gas or diesel fired power stations, steel works or petroleum refineries.
  • the carbon dioxide may be treated to remove some or all of any gaseous contaminants that may be present in the stream.
  • the reaction of sodium chloride and carbon dioxide to produce soda ash is catalysed by ammonia, and in the present invention at least a portion of the ammonia that is used as the catalyst is regenerated from ammonium chloride produced during the reaction.
  • the ammonium chloride produced during the reaction will ideally be filtered, after collection of the sodium bicarbonate, by a high pressure filter such as a reverse osmosis membrane to provide purified water that can be reused, and at the same time to concentrate the remaining ammonium chloride solution.
  • the concentrated ammonium chloride solution will then be the solution treated with a base to regenerate ammonia suitable for reuse in the reaction, and in one form the base will be an anion exchange resin.
  • the regenerated ammonia may make up at least 10%, and preferably somewhere between 20% and 80%, of the ammonia required for the reaction. Ideally, all of the ammonia regenerated will be returned to the reactor, and an amount of fresh ammonia will be added to the reactor to make up the ammonia solution strength as required for the reaction. It will thus be appreciated that the amount of fresh ammonia used in the reactor will be dependent upon the operating parameters of each individual operation that might utilise the process of the present invention.
  • the basic chemical reactions involved in the process of the present invention are similar to the Solvay process which is currently used industrially to produce soda ash.
  • the traditional Solvay process produces soda ash from concentrated brine (as a source of sodium chloride (NaCI)) and from limestone (as a source of calcium carbonate (CaCOs)).
  • the traditional Solvay process is an energy intensive process. Firstly, the reactant carbon dioxide gas is obtained by heating limestone in a kiln to drive off carbon dioxide gas. This is an energy intensive step, not only consuming a large amount of thermal energy (typically, it requires 2.2-2.8 GJ/ton of soda ash), but also producing surplus greenhouse gas carbon dioxide (typically, 200-400 kg/ton soda ash) which is usually released to the atmosphere.
  • the brine used as a starting material in the traditional Solvay process is a concentrated brine solution, typically having a salt concentration of about 300 g/L.
  • brine having a significantly lower salt concentration can successfully be used in a modified Solvay process to produce soda ash. This leads to the environmentally positive outcome of being able to use brine waste as a starting material in soda ash production.
  • the brine waste may be a waste stream from a desalination plant.
  • Desalination plants are used to reduce the salt concentration of sea water, brackish water, saline industrial waste water, and the like.
  • the desalination plant may be a reverse osmosis desalination plant, in which case, the brine waste may have a sodium chloride concentration of greater than about 50 g/L and less than about 250 g/L.
  • the sodium chloride concentration of the brine waste is greater than about 50g/L and less than about 250 g/L.
  • that lower limit of the range may be 60 g/L, 70 g/L, 80 g/L, 90 g/L, or 100 g/L.
  • the present invention therefore also provides a process for producing soda ash, the process including the steps of: a) providing brine waste having a sodium chloride concentration of between about 50 g/L and about 250 g/L; b) treating the brine waste to remove at least some of any undesired inorganic cations present to provide pre-treated brine waste; c) reacting the pre-treated brine waste with carbon dioxide in the presence of ammonia, at least a portion of which is regenerated ammonia from step (g); d) separating sodium bicarbonate produced during the reaction of the brine waste with carbon dioxide from the reaction mixture to provide collected sodium bicarbonate and a first mother liquor containing ammonium chloride; e) heating the collected sodium bicarbonate to produce soda ash; f) filtering the first mother liquor to produce purified water and a second mother liquor containing concentrated ammonium chloride; and g) treating the second mother liquor to regenerate ammonia suitable for use in the reaction of step (c).
  • Soda ash is an important industrial chemical. Soda ash is used to regulate pH in many chemical process streams. For example, it is the most widely used fixed alkali for the manufacture of other alkali products, sodium salts, glass, soap, sodium silicates, detergent, bicarbonates, bichromates, cellulose and rayon, iron and steel, aluminium, cleaning compounds, textiles and dyestuffs, drugs and many other materials. It is also used as an alkali for household purposes and as washing powder by laundries. It is used in the manufacture of glass, chemicals, such as sodium silicates and sodium phosphates, the pulp and paper industries, the manufacture of detergents and for the treatment of water. The superior buffering capacity of soda ash versus caustic soda offers advantages in adjusting plant wastewater pH ranges.
  • the present invention provides a more sustainable approach to soda ash production. Firstly, the process of the present invention utilises brine waste as a starting material, thereby ameliorating the need to dispose of brine waste from desalination plants in the typical manner. Secondly, the present invention is also able to release at least a small portion of the water contained in a brine waste as purified water for re-use. Thirdly, the present invention can use carbon dioxide that is obtained from emissions from a combustion source, such as coal or gas or diesel fired power station, steel works or petroleum refinery, as a starting material for the reaction. Finally, and in contrast with the traditional
  • Figure 1 is a general flow diagram of a process for producing soda ash according to the present invention
  • Figure 2 is a detailed flow diagram of a process for producing soda ash according to the present invention
  • Figure 3 is a graph showing a comparison of different concentrations of sodium carbonate for use as a regenerant solution for ion exchange resin
  • Figure 4 is a plot of sodium bicarbonate (NaHCO 3 ) conversion rates with varying initial brine concentrations.
  • the present invention provides a process for producing soda ash from brine waste.
  • the process includes treating brine waste with carbon dioxide and ammonia under conditions to produce soda ash.
  • soda ash means a composition that contains predominantly sodium carbonate (Na2CO3). Soda ash may not be pure sodium carbonate and may contain other compounds including, for example, sodium bicarbonate (NaHCO 3 ).
  • brine waste 10 from a desalination plant 12 is fed into a reaction vessel 14.
  • the brine waste 10 may be subjected to the process of the present invention on-site at a desalination plant, or it may be stored and/or packaged for transportation to an off-site processing facility.
  • the brine waste is ideally treated on-site at a desalination plant.
  • brine waste could be obtained from waste streams from other desalination plants, including plants that use thermal desalination processes such as Multistage Flash Distillation (MFD), Multiple Effect Distillation (MED) and Mechanical Vapour Compression (MVC). These processes all generate concentrated brine streams that can be utilised for soda ash production as described herein.
  • MFD Multistage Flash Distillation
  • MED Multiple Effect Distillation
  • MVC Mechanical Vapour Compression
  • Carbon dioxide 16 that is obtained from emissions from a combustion source 18 is introduced into the reaction vessel 14 and passed through the brine waste 10 in the vessel.
  • the carbon dioxide 16 is ideally obtained from emissions from coal or gas or diesel fired power stations, steel works, petroleum refineries, and the like.
  • Ammonia 20 is also introduced into the reaction vessel 14 and passed through the brine waste 10. Typically, ammonia 20 is introduced into the reaction vessel 14 first followed by introduction of the carbon dioxide 16.
  • the overall reaction process is:
  • the reaction of the brine waste 10 with carbon dioxide 16 and ammonia 20 can also be carried out in two stages. In the first stage, ammonia 20 would be bubbled through the brine waste 10 so that it is absorbed by the brine waste to produce ammoniated brine. In the second stage, carbon dioxide 16 would be bubbled through the ammoniated brine.
  • sodium bicarbonate (NaHCO 3 ) precipitates out of solution.
  • the sodium bicarbonate precipitates because in a basic solution, sodium bicarbonate is less water-soluble than sodium chloride.
  • the ammonia (NH 3 ) buffers the solution at a basic pH; without the ammonia, a hydrochloric acid by-product would render the solution acidic, and arrest the precipitation.
  • the sodium bicarbonate that precipitates out in reaction is filtered using a filter 24 and then dried to form a dried sodium bicarbonate precipitate 22.
  • This dried sodium bicarbonate precipitate 22 is subsequently converted to soda ash by calcination (160 - 230 0 C), producing water and carbon dioxide as by-products, as per the following process:
  • the water and carbon dioxide produced during this final calcination step may be captured and re-used as a starting material in the process or they may be fed directly into the process as required.
  • the solution remaining from the reaction vessel 14 contains ammonium chloride (NH 4 CI).
  • the mother liquor obtained after filtration is reacted with quicklime (calcium oxide (CaO)) left over from the calcination step (CaCO 3 -> CO 2 + CaO) to regenerate ammonia which is recycled back to the initial brine solution.
  • quicklime calcium oxide (CaO)
  • CaCO 3 -> CO 2 + CaO quicklime
  • this step generates large amounts of calcium chloride solids that are typically disposed of into a waterway.
  • ammonia is regenerated from the ammonium chloride by passing the solution containing ammonium chloride through a regeneration step such as an anion exchange resin 26. No solid wastes are generated in this regeneration step and, therefore, the environmental impact of the process is further reduced.
  • the process can also include treating the brine waste 10 to remove at least some of any undesired inorganic cations present in the brine waste prior to its treatment in the reactor 14 with carbon dioxide and ammonia.
  • undesired inorganic cations are ions that may interfere with the soda ash production process include, but are not limited to, calcium, magnesium or strontium ions.
  • the flow diagram of Figure 2 shows the brine waste moving through dual cation exchange treatment processes, where the brine waste is treated with a binding agent that selectively binds calcium ions, a binding agent that selectively binds magnesium ions, and/or a binding agent that selectively binds strontium ions.
  • the binding agent is a cation exchange resin.
  • the cation exchange resin may be AMBERLITE IRC748, which is an iminodiacetic acid chelating cation exchange resin with high selectivity for calcium, magnesium and strontium.
  • This step may alternatively be an activated carbon absorption step, an advanced oxidation step, or a combination of all of these described steps.
  • the carbon dioxide gas 16 used in the reaction may be pumped directly from its source to the reaction vessel 14 containing the ammoniated brine solution.
  • the carbon dioxide gas may be captured off site and stored in an appropriate vessel (such as a cylinder) for transport to the site where the reaction is carried out.
  • the carbon dioxide gas when the carbon dioxide gas is derived from a waste stream, it may be desirable to scrub the waste stream to remove some or all of any gasesous contaminants that may be present in the stream.
  • gaseous contaminants examples include nitrogen oxides (NO x ) and sulphur dioxide (SO 2 ).
  • NO x nitrogen oxides
  • SO 2 sulphur dioxide
  • the impurities NO 2 and SO 2 can be converted into nitrate ion and sulphate ions.
  • the sodium salts of these ions are more soluble than sodium bicarbonate so the salts remain in solution and can be finally removed by, for example, membrane filtration before the reuse of water.
  • At least a portion of the ammonia 20 that is used to treat the brine waste may be obtained from any suitable source. However, it is possible to regenerate and then reuse ammonia from ammonium chloride produced during the reaction in the reaction vessel 14, and thus it is advantageous to re-use the ammonia regenerated in this manner, such that at least a portion of the ammonia used in the reaction is regenerated ammonia.
  • the ammonium chloride produced during the reaction is filtered (after filtration 26 to collect the sodium bicarbonate formed from the brine waste, the carbon dioxide and the ammonia in vessel 14) in a membrane filter 27 to concentrate the ammonium chloride solution.
  • This concentrate may then be treated with a base in an ion exchange process 26 to generate ammonia suitable for reuse in the reaction.
  • Any suitable base may be used in this ion exchange process.
  • the base is a weak base anion exchange resin.
  • the concentrated ammonium chloride may be passed through a column containing an anion exchange resin, such as AMBERLYST A23 or AMBERLITE IR 45, which are highly porous granular weak base anion exchange resins, both showing sufficient alkali capacity to be used for the purpose of ammonia regeneration, or such as AMBERLITE IRA 400, a strong base anion exchange resin.
  • an anion exchange resin such as AMBERLYST A23 or AMBERLITE IR 45, which are highly porous granular weak base anion exchange resins, both showing sufficient alkali capacity to be used for the purpose of ammonia regeneration, or such as AMBERLITE IRA 400, a strong base anion exchange resin.
  • the chloride ions in the concentrate will be absorbed, and the hydroxyl ions will be exchanged to the concentrate from the resin.
  • the effluent of the anion exchange resin column contains ammonia with high alkalinity, and can be returned (via stream 29) back to the carbonisation reactor.
  • Sodium carbonate may also be used to itself regenerate spent anion exchange resin, as represented schematically in Figure 2 by the stage 31.
  • the weak base anion exchange resins can be efficiently regenerated by much weaker sodium carbonate solution, such as 1 % of sodium carbonate (noting that the recommended regeneration concentration is 5% sodium carbonate).
  • the present invention avoids the need to use energy intensive lime milk and steam distillation for ammonia regeneration, as in the traditional Solvay process.
  • the weak base anion exchange resin can be regenerated by weak waste alkali which is available from several industries, such as alkaline fly ash from brown coal combustion or slag from steel mill.
  • testwork has been conducted on the weak base anion exchange resins to confirm that they exhibit the most potential to be regenerated by weak waste alkali.
  • Gas mixture - gas cylinders supplying CO2, N 2 , SO 2 and NO2 were set up with mass flow controllers (based on the "multibus" concept) for certain flow rates and for desired mixing ratios.
  • the percentage of CO 2 was set up at 5%, 7.5%, 10% and 15% to simulate expected industrial conditions, and accordingly, the percentages of N 2 were set up at 95%, 92.5%, 90% and 85% respectively), following which the gas tube was connected to the gas washing bottle.
  • the experimental work showed the following relationship between CO 2 concentrations and NaCI concentrations on the process reaction rate, showing an ideal reaction rate at CO 2 concentrations above about 7.5% and NaCI concentrations above about 147g/L.
  • Figure 4 represents the conversion rates to sodium bicarbonate based on to its initial Na + concentrations.
  • Figure 4 shows that the conversion rates, represented as (C 0 -C e )/C 0 , increased with increasing Na + concentration in a logarithmic shaped trend.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Treatment Of Water By Ion Exchange (AREA)
  • Treating Waste Gases (AREA)

Abstract

Procédé d'obtention de carbonate de sodium à partir de saumure résiduaire. Ce procédé consiste à faire réagir de la saumure résiduaire avec du dioxyde de carbone et de l'ammonium pour produire du carbonate de sodium, une partie au moins de l'ammoniac étant régénérée à partir du chlorure d'ammonium produit pendant la réaction, la régénération étant dans l'idéal obtenue au moyen d'une résine échangeuse d'anions de type base faible.
PCT/AU2009/001512 2008-11-21 2009-11-20 Utilisation de déchets de dessalement WO2010057261A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
JP2011536704A JP2012509237A (ja) 2008-11-21 2009-11-20 脱塩廃液の利用
ES09827050.7T ES2553969T3 (es) 2008-11-21 2009-11-20 Utilización de desechos de desalinización
EP09827050.7A EP2361224B1 (fr) 2008-11-21 2009-11-20 Utilisation de déchets de dessalement
CA2744264A CA2744264A1 (fr) 2008-11-21 2009-11-20 Utilisation de dechets de dessalement
CN2009801544359A CN102282106B (zh) 2008-11-21 2009-11-20 淡化废水的利用
AU2009317875A AU2009317875B2 (en) 2008-11-21 2009-11-20 Utilisation of desalination waste
US13/130,423 US8741249B2 (en) 2008-11-21 2009-11-20 Utilisation of desalination waste
IL213005A IL213005A (en) 2008-11-21 2011-05-19 Process for making sodium carbonate from desalinated waste

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2008906021A AU2008906021A0 (en) 2008-11-21 Utilisation of desalination waste
AU2008906021 2008-11-21

Publications (1)

Publication Number Publication Date
WO2010057261A1 true WO2010057261A1 (fr) 2010-05-27

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PCT/AU2009/001512 WO2010057261A1 (fr) 2008-11-21 2009-11-20 Utilisation de déchets de dessalement

Country Status (9)

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US (1) US8741249B2 (fr)
EP (1) EP2361224B1 (fr)
JP (1) JP2012509237A (fr)
CN (1) CN102282106B (fr)
AU (1) AU2009317875B2 (fr)
CA (1) CA2744264A1 (fr)
ES (1) ES2553969T3 (fr)
IL (1) IL213005A (fr)
WO (1) WO2010057261A1 (fr)

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* Cited by examiner, † Cited by third party
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WO2012113958A1 (fr) * 2011-02-23 2012-08-30 Abengoa Water, S. L. U. Procédé de traitement de saumure
WO2013126092A2 (fr) * 2012-02-22 2013-08-29 Idea International Investment And Development Company Procédé de production de carbonate de sodium et de chlorure de calcium
CN104556155A (zh) * 2014-12-25 2015-04-29 唐山三友化工股份有限公司 利用氯碱尾料和氨碱尾料生产纯碱的方法
EP3006400A1 (fr) * 2014-10-09 2016-04-13 Solvay SA Procédé de production d'ammoniac
WO2017029509A1 (fr) 2015-08-18 2017-02-23 United Arab Emirates University Procédé de capture de dioxyde de carbone et de dessalement

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CN103435075B (zh) * 2013-08-20 2015-04-22 湖北双环科技股份有限公司 碳化塔水洗方法及其装置
KR101375987B1 (ko) * 2013-09-10 2014-03-19 소재한 해수담수화 역삼투압 농축 폐액과 합성천연가스 부생가스를 이용한 소다회의 제조방법
WO2015085353A1 (fr) * 2013-12-12 2015-06-18 Reid Systems (Australia) Pty Ltd Procédé et appareil pour éliminer du dioxyde de carbone provenant de gaz de carneau
US9475000B2 (en) * 2014-09-11 2016-10-25 Qatar University Carbon dioxide mineralization using reject brine
RU2647931C2 (ru) * 2015-11-27 2018-03-21 Федеральное Казенное Предприятие "Авангард" Способ переработки твердых отходов производства кальцинированной соды аммиачным методом
US11247940B2 (en) 2016-10-26 2022-02-15 The Regents Of The University Of California Efficient integration of manufacturing of upcycled concrete product into power plants
CN107200337B (zh) * 2017-05-25 2019-05-07 中国中轻国际工程有限公司 一种含小苏打硝盐卤水生产纯碱工艺
WO2019006352A1 (fr) * 2017-06-30 2019-01-03 The Regents Of The University Of California Minéralisation de co2 dans de l'eau d'effluent produite et industrielle par carbonatation à variation de ph
BR112020003106A2 (pt) 2017-08-14 2020-09-01 The Regents Of The University Of California métodos de fabricação e produtos de concreto
CN110407351B (zh) * 2018-04-27 2022-07-12 国家能源投资集团有限责任公司 一种含盐废水的处理方法
US11384029B2 (en) 2019-03-18 2022-07-12 The Regents Of The University Of California Formulations and processing of cementitious components to meet target strength and CO2 uptake criteria
CN111977673A (zh) * 2020-07-29 2020-11-24 山东海天生物化工有限公司 一种小苏打生产工艺
CN112374509B (zh) * 2020-11-19 2023-05-09 山东海天生物化工有限公司 一种纯碱生产用精盐水的精制工艺

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US1570299A (en) * 1922-05-01 1926-01-19 Pittsburgh Plate Glass Co Ammonia soda process
GB994601A (en) * 1962-08-13 1965-06-10 Solvay Process for the manufacture of sodium carbonate
US3368866A (en) * 1962-08-13 1968-02-13 Solvay Process for the manufacture of sodium carbonate
US6180012B1 (en) * 1997-03-19 2001-01-30 Paul I. Rongved Sea water desalination using CO2 gas from combustion exhaust
WO2001028925A1 (fr) * 1999-10-21 2001-04-26 Airborne Industrial Minerals Inc. Formulation de sulfate de potassium, de carbonate sodium et de bicarbonate de sodium tiree de saumures a base de carbonate neutre de potassium
WO2001096243A1 (fr) * 2000-06-16 2001-12-20 Paul Rongved Procede de dessalement d'eau de mer
WO2007094691A1 (fr) * 2006-02-17 2007-08-23 Enpro As Procédé de traitement d'eau saline, et de dioxyde de carbone
WO2007139392A1 (fr) * 2006-05-30 2007-12-06 Enpro As Procédé solvay modifié et utilisations de celui-ci pour traiter des flux de gaz contenant du co2 et pour la désalinisation
WO2008110405A2 (fr) * 2007-03-15 2008-09-18 Silicon Fire Ag Procédé et dispositif de liaison de co2 gazeux et de traitement de gaz de combustion à l'aide de composés carbonate de sodium

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012113958A1 (fr) * 2011-02-23 2012-08-30 Abengoa Water, S. L. U. Procédé de traitement de saumure
ES2390166A1 (es) * 2011-02-23 2012-11-07 Abengoa Water, S.L.U. Procedimiento de tratamiento de salmuera.
WO2013126092A2 (fr) * 2012-02-22 2013-08-29 Idea International Investment And Development Company Procédé de production de carbonate de sodium et de chlorure de calcium
WO2013126092A3 (fr) * 2012-02-22 2014-01-03 Idea International Investment And Development Company Procédé de production de carbonate de sodium et de chlorure de calcium
EP3006400A1 (fr) * 2014-10-09 2016-04-13 Solvay SA Procédé de production d'ammoniac
WO2016055367A1 (fr) * 2014-10-09 2016-04-14 Solvay Sa Procédé de production d'ammoniac
CN106999853A (zh) * 2014-10-09 2017-08-01 索尔维公司 用于生产氨的方法
CN104556155A (zh) * 2014-12-25 2015-04-29 唐山三友化工股份有限公司 利用氯碱尾料和氨碱尾料生产纯碱的方法
WO2017029509A1 (fr) 2015-08-18 2017-02-23 United Arab Emirates University Procédé de capture de dioxyde de carbone et de dessalement

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EP2361224A4 (fr) 2013-03-06
US8741249B2 (en) 2014-06-03
US20110268633A1 (en) 2011-11-03
AU2009317875A1 (en) 2010-05-27
IL213005A (en) 2016-02-29
ES2553969T3 (es) 2015-12-15
EP2361224B1 (fr) 2015-07-08
CN102282106A (zh) 2011-12-14
AU2009317875B2 (en) 2015-09-17
EP2361224A1 (fr) 2011-08-31
CN102282106B (zh) 2013-12-04
IL213005A0 (en) 2011-07-31
CA2744264A1 (fr) 2010-05-27

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