US3332470A - Method for concentrating solutions - Google Patents

Method for concentrating solutions Download PDF

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Publication number
US3332470A
US3332470A US522967A US52296766A US3332470A US 3332470 A US3332470 A US 3332470A US 522967 A US522967 A US 522967A US 52296766 A US52296766 A US 52296766A US 3332470 A US3332470 A US 3332470A
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Prior art keywords
liquor
line
solute
effect
concentrator
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Expired - Lifetime
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US522967A
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English (en)
Inventor
Anthony N Chirico
Jay D Dockendorff
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Chicago Bridge and Iron Co
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Chicago Bridge and Iron Co
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Priority to US522967A priority Critical patent/US3332470A/en
Priority to GB3613/67A priority patent/GB1113580A/en
Priority to NL6701170A priority patent/NL6701170A/xx
Priority to BE693174D priority patent/BE693174A/xx
Priority to FR92419A priority patent/FR1522265A/fr
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Publication of US3332470A publication Critical patent/US3332470A/en
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D1/00—Oxides or hydroxides of sodium, potassium or alkali metals in general
    • C01D1/04—Hydroxides
    • C01D1/42—Concentration; Dehydration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/26—Multiple-effect evaporating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0018—Evaporation of components of the mixture to be separated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S159/00—Concentrating evaporators
    • Y10S159/08—Multieffect or multistage
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S159/00—Concentrating evaporators
    • Y10S159/25—Decant, press, centrifuge
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S159/00—Concentrating evaporators
    • Y10S159/34—Caustic

Definitions

  • This invention relates to a method for concentrating a solution and separating crystals therefrom.
  • this invention relates to a method for concentrating a solution having two or more chemical solutcs, crystallizing at least one solute, and separating the crystals from the remaining concentrated solution.
  • the invention is described hereinbelow in detail with reference to electrolytic caustic soda, but it should be understood that the invention is equally applicable to other solutions having chemically diderent constituents.
  • the brine charge is partly converted through electrolysis into caustic soda.
  • the liquor withdrawn from the electrolytic cells typically comprises about 8 to 11% sodium hydroxide, 13 to 17% sodium chloride, and the balance water.
  • the caustic soda is separated from the salt by concentrating the cell liquor in a multiple effect evaporator system to crystallize most of the salt, which is then separated from the mother liquor.
  • This invention has as its purpose to provide a preconcentrator for use in treating the feed liquor in combination with the multiple-effect evaporator, whereby substantial economy is realized both with respect to operating costs and capital costs.
  • Regenerative heaters 12, 14 and 16 are heated by indirect heat exchange by the vapors flashed in the several dash coolers 44, 42 and 40 respectively, and condensed vapors from the heat exchanger 91 of the first eiect 58 of the multiple effect evaporator system are recycled by line 99 to heat regenerative heater 18 by liquid to liquid indirect heat exchange, as described hereinbelow in greater detail.
  • the cell liquor flows from line to heater 12, and then through line 13 to heater 14, then via line 15 to heater 16, and then through line 17 to heater 18.
  • the pressure in the regenerative heaters is sufficient to suppress boiling of the liquor and also is suicient to transport the cell liquor through the regenerative heaters to the pre-concentrator.
  • the number of regenerative heaters employed in the operation can vary, depending upon a number of factors, such as size and the operating temperature range, but the number of heaters should be suiicient to optimize heating with respect to the subsequent ash cooling stages. However, it is preferable to employ a plurality of regenerative heaters in that, in bringing the liquor to the desired elevated temperature, a lesser amount of outside heat supply would be required.
  • the cell liquor which is now at an elevated temperature, is passed via line to preheater 22.
  • Steam is supplied to the preheater 22 from a suitable boiler (not shown) via line 24 and branch line 26, to heat the liquor to a high temperature for admission 3,332,470 Patented July 25, 1957 ice to the pre-concentrator.
  • the steam condensate from preheater 22 is fed by line 29 to line 36 which returns it to the boiler.
  • this separate preheater, heated by a steam source may be omitted.
  • the pre-concentrator is desirably a falling ⁇ film type evaporator comprising a vertical shell and tube heat exchanger 32 with tubes communicating with a vapor body 33 disposed below the heat exchanger. Steam is supplied to the shell side of the heat exchanger via line 24 and branch line 31. Because the liquor is maintained at a high temperature and under pressure, the liquor shoots rapidly through the vertical tubes and a substantial amount of liquid is evaporated in the pre-concentrator.
  • the vapors generated are passed from the vapor body 33 through a vapor outlet conduit 34 for use as heating medium in the multiple eiect evaporator, described hereinbelow, and the condensate from the preheater 22 and preconcentrator 30 is returned to the boiler by means of a return line 36.
  • the hot liquor which now is relatively more concentrated because of evaporation in the pre-concentrator, is then passed through line 38 to a plurality of ash coolers 40, 42, and 44 where liash vaporization occurs.
  • the ternperature of the liquor and the operating pressure are reduced in the flash coolers, each successive flash cooler being at a lower temperature and pressure than the preceding one.
  • the liquor enters the rst flash cooler 40, which is operated at a lower pressure as compared to the pre-concentrator and the solution adiabatically cools to the boiling temperature corresponding to the pressure existing in the vessel.
  • the vapor generated is passed through branch steam line 46 to regenerative heater 16, thereby heating unit 16 by indirect heat exchange.
  • the concentrated liquor is then passed through line 41 to liiash cooler 42, maintained at a lower pressure than flash cooler 40, where further evaporation occurs, and similarly, vapor generated is passed via line 48 to regenerative heater 14 to heat that unit by indirect heat exchange. Still further evaporation of the liquor occurs in ash cooler 44, maintained at a still lower pressure, to which the liquor is fed by line 43 and the steam generated is conducted through line 50 to heat regenerative heater 12 by indirect heat exchange.
  • the resultant cooling and vaporization of some of the solvent will supersaturate the solution with respect to the sodium chloride, and sodium chloride crystals are produced which serve as nuclei or seeds to eiect growth in the multiple effect evaporators.
  • This stage of the process is particularly important in that controlled nucleation or seed generation affects the size and habit of the crystals developed in the multiple eiiect evaporators, which is important in order to achieve optimum crystals and to improve the plant efticiency as aected by the separation of the crystallized solute from the mother liquor.
  • the system of regenerative heaters and Iflash coolers shown in the drawing is purely illustrative of how savings in capital and operating costs can be realized, and the number, use, and arrangement of such units will depend upon the conditions encountered for each particular installation, such as steam pressure available, the degree of concentration of the feed liquor, the degree of concentration desired to control nucleation, and the like.
  • the mother liquor from the last ash cooler 44 flows from line 52 to the multiple-effect evaporator system, and, as illustrated, the eiects are operated at successively lower ltemperatures.
  • the second-effect evaporator 54, the third-eiTect evaporator 56, and the first-effect evaporator 58 all of conventional forced circulation design, and the mother liquor is conducted via line 52 to the second effect of a three-effect evaporator system, but it should be understood that the mother liquor may pass first to any of the three evaporators.
  • the numbering employed in referring to the particular effect in the system is in order of decreasing operating pressure.
  • the feed liquor which contains sodium chloride crystal nuclei, is fed to the second effect of the multi-effect evaporator system which is operated at a subatmospheric pressure.
  • a recirculation system is provided for each evaporator-crystallizer effect.
  • the recirculation system for the second effect 54 comprises slurry outlet line 60, a recirculation pump 62, line 61 from the pump to heat exchanger 63 and a return slurry inlet line 64 which results in admixture of slurry with feed liquor from line S2.
  • the recirculation system for the first effect 58 comprises slurry outlet line 90, a slurry recirculation pump 92 which feeds slurry by line 94 to heat exchanger 91 from which line 96 feeds it to first effect S8.
  • the recirculation system for the third effect 56 comprises outlet line 130 which feeds slurry to pump 131 which by line 132 feeds the slurry to heat exchanger 133 from which line 134 feeds the slurry to the third effect 56.
  • Magma comprising a slurry of product crystals of desired size suspended in mother liquor is discharged from the crystallization section of the evaporator-crystaliizer 54 and transferred to slurry tank 70 through line 71.
  • the slurry tank 70 is desirably provided with a conical bottom or trim-conical bottom, and the salt crystals settle into the conicai bottom portion and are removed via line 72.
  • the liquor is now relatively more concentrated, and the mother liquor, having an increased content of caustic soda as compared to the original feed liquor from the electrolytic cell, but still containing a substantial percentage of sodium chloride, is decanted or Withdrawn from the slurry tank as by a suitable pump means (not shown) through line 76 to the third-effect evaporator 56 of the multiple-stage evaporator system maintained under subatmospheric pressure.
  • the liquor is concentrated by evaporation and, under the operating conditions, an amount of salt crystallizes out of solution and the slurry is Withdrawn through outlet means 78.
  • the vapors generated pass from the vapor zone of the crystallizer via line 80 to barometric condenser 82 which maintains a vacuum in this third effect. Similar recirculation means described above with respect to evaporator effect 54 are provided for the third effect 56.
  • mother liquor is removed by line 130 and pump 131 and sent through line 132, through heat exchanger 133 and by line 134 to third effect S6.
  • Hot condensate from heat exchanger 63 is fed by line 106 to heat exchanger 133.
  • Condensate from heat exchanger 133 is sent by line 135 to storage.
  • the magma containing crystals of desired size is passed to a second slurry tank 84 through line 73.
  • Salt crystals which settle in the lower conical portion of the :slurry tank are withdrawn through line 88 to the first slurry tank 70.
  • the salt crystals from slurry tank 84 -are washed by the slurry in tank 70, thereby removing some of the sodium hydroxide in the salt.
  • the relatively clear mother liquor containing a still higher percentage of caustic soda, is withdrawn from tank 84 via line 88 to the first effect 58 of the multiple-stage evaporator system maintained at about atmospheric pressure.
  • the liquor is withdrawn from evaporator effect 58 via line 90 and is recirculated through suitable recirculating means, including pump 92 and line 94 where it admixes with feed from line 88, and is fed through heat exchanger 91 and introduced to the evaporator through line 96.
  • Vapors generated in pre-concentrator 30 are transported from the v apor body 33 by line 34 to the heat exchanger 91 for use as the heating medium for effect 58 by indirect heat exchange.
  • the vapor condensate from heat exchanger 91 is fed by line 99 to heater 18 from which it is withdrawn by line 140 and fed to heater 16 from which it is fed by line 141 to heater 14 and from it by line 142 to heater 12.
  • Line 143 takes the condensate from heater 12 and carries it to storage. Evaporation occurs in first effect 58 thereby resulting in additional concentration and crystal growth.
  • the vapors generated are withdrawn from the vapor space of the first effect evaporator 58 through line 98 and pass to the heat exchanger 63 associated with the second effect 54 to supply heat for that evaporator. Vapor condensate from heat exchanger 63 is passed through line 106 to heat exchanger 133.
  • the solution withdrawn from the first-effect evaporator 58 is relatively concentrated with respect to caustic soda and now contains a very low percentage of sodium chloride.
  • This concentrated solution is Withdrawn through branch line 102, leading from line 96, to a flash evaporator 103 which may have the same general construction Ias the evaporator effects in the multiple-stage evaporator system.
  • the fiash evaporator 103 is operated under subatmospheric conditions and at a temperature lower than the temperature in the first effect 53 whereby fiash vaporization occurs.
  • the vapors generated are passed via line 104 directly to the 'barometric condenser 82 and the condensate reprocessed.
  • the liquor in fiash evaporator 103 is recirculated through line 110 ⁇ at the bottom of the vessel by pump means 112 and return line 114.
  • the substantially crystal-free liquor, circulating in the recirculating means is Withdrawn through branch line 116 to slurry tank 118. Salt crystals in the liquor settle out under gravity and are Withdrawn from the conical bottom portion via line 120.
  • the salt withdrawn from slurry tank 118 is washed by the salt and mother liquor in slurry tank 84, thereby effecting progressive washings of the crystal sludge in each of the slurry tanks.
  • the salt crystals Withdrawn from the bottom tank in this successive arrangement is passed to a suitable centrifuge 122 for further separation of the salt from the mother liquor, whereby the salt may be recovered and returned to the electrolytic cell for further .processing in the manufacture of caustic soda.
  • the feed liquor from the electrolytic cell which typically has a temperature of about 140 to 150 F.
  • the feed liquor from the electrolytic cell which typically has a temperature of about 140 to 150 F.
  • the feed liquor is fed from line 10 to the regenerative heaters.
  • the incoming cell liquor is heated by indirect heat exchange, by the vapors generated in the ash coolers.
  • the feed liquor is heated in regenerative heater 12 to a temperature of about 200 F., and further raised to about 227 F. in heater 14, and further heated in heater 16 to temperature of .257 F.
  • the cell liquor is further elevated in temperature in heater 18 to about 267 F.
  • the cell liquor then flows under pressure to preheater 22 where the liquor is heated to about 329 F. by means of indirect heat exchange with steam from a suitable steam source from lines 24 and 26.
  • the cell liquor at this elevated temperature and under sufficient pressure to suppress boiling, e.g. p.s.i.g., is
  • the pre-concentrator for example, of the falling film type, may be maintained at a pressure of about 65 p.s.i.g., and the vapors generated at 312 F. and 65 .p.s.i.g. are withdrawn through line 34 to heat exchanger 91 to heat the first effect 58 of the multiple effect evaporator system.
  • the liquor withdrawn from the pre-concentrator through line 38 is now at a higher concentration, e.g. 13.6% caustic soda, but the concentration and temperature conditions are controlled so that no crystallization occurs until the cell liquor is treated in the ash coolers.
  • concentration and temperature conditions are controlled so that no crystallization occurs until the cell liquor is treated in the ash coolers.
  • salt deposits gradually accumulate on the interior walls of the vessels.
  • operations must be discontinued periodically for removing the salt.
  • this disadvantage is overcome in that no crystallization occurs in the pre-concentrating stage of the operation.
  • the liquor is cooled in the first ash cooler 40, which is operated at a slightly elevated pressure of about 35 p.s.i.g., and a temperature of about 291 F.
  • fiash cooler 42 may be operated at a temperature of about 261 F. and a pressure of 25 p.s.i.g., and cooler 44 operated at a temperature of about 230 F. and at atmospheric pressure, As explained above, crystallization of sodium chloride occurs in one or more of the flash coolers to generate seed for the multiple-effect evaporators.
  • the liquor containing some sodium chloride crystals is then passed to the second effect of the multiple-stage evaporator system.
  • This effect 54 is operated under vacuum and at a relatively lower temperature of about 192 F.
  • the composition of the slurry withdrawn through outlet line 71 comprises about 23% caustic soda, 17% sodium chloride, and the balance water.
  • the mother liquor passed to the third effect 56 from slurry tank 70 is evaporated under a vacuum and at a still lower temperature of about 147 F.
  • the slurry Withdrawn comprises about 32% sodium hydroxide, 12% sodium chloride, and 56% water.
  • Mother liquor passed to the first effect 58 from slurry tank 84 is treated at an elevated temperature of about 282 F. and atmospheric pressure.
  • the relatively clear mother liquor having a low sodium chloride content is withdrawn from the first effect and passed to the flash evaporator 103 and then to a third slurry tank.
  • the composition of the liquor comprises about 49.5% caustic soda and 2-3% sodium chloride.
  • the slurry is passed to the caustic coolers and cooled to about 80 F. to cause further crystallization of salt, thereby resulting in a solution containing about 1% salt.
  • a method for recovering a first solute from liquor and recovering liquor relatively concentrated with respect to a second solute comprising:
  • a method according to claim 1 including a plurality of regenerative heaters being interconnected for series flow, each of said regenerative heaters being operated at successively higher temperatures; and a plurality of flash coolers being interconnected for series flow, each of said flash coolers being operated at successively lower temperatures, whereby the vapors generated in each of said flash coolers are employed as heating medium for said feed liquor introduced to said regenerative heaters in inverse order.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
US522967A 1966-01-25 1966-01-25 Method for concentrating solutions Expired - Lifetime US3332470A (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
US522967A US3332470A (en) 1966-01-25 1966-01-25 Method for concentrating solutions
GB3613/67A GB1113580A (en) 1966-01-25 1967-01-24 Separation of crystals from solutions,by evaporation of solvent
NL6701170A NL6701170A (ja) 1966-01-25 1967-01-25
BE693174D BE693174A (ja) 1966-01-25 1967-01-25
FR92419A FR1522265A (fr) 1966-01-25 1967-01-25 Procédé perfectionné de concentration de solutions

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US522967A US3332470A (en) 1966-01-25 1966-01-25 Method for concentrating solutions

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Cited By (29)

* Cited by examiner, † Cited by third party
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US3738411A (en) * 1969-08-05 1973-06-12 Tatabanyai Szenbanyak Treatment of aluminate digester liquor
US3912578A (en) * 1973-01-22 1975-10-14 United States Steel Corp Apparatus for and a method of purifying waste fluid
US4087253A (en) * 1975-03-28 1978-05-02 Rhone-Poulenc Industries Method of obtaining caustic soda from a sodium chloride liquor containing sulphate ions recovered from an electrolytic cell
FR2384035A1 (fr) * 1977-03-15 1978-10-13 Asahi Glass Co Ltd Procede de concentration d'une solution d'alcali caustique obtenue par electrolyse du type a membrane echangeur d'ion
US4441958A (en) * 1981-01-27 1984-04-10 Giampaolo Teucci Forced-circulation evaporator plant
EP0114974A2 (de) * 1983-01-28 1984-08-08 Hüls Aktiengesellschaft Verfahren zum Zersetzen natronhaltiger Mehrfachsalze
US4981555A (en) * 1988-10-12 1991-01-01 Metallgesellschaft Ag Process and apparatus for concentrating a solution
US5209828A (en) * 1991-12-23 1993-05-11 Mobil Oil Corporation System for concentrating a spent caustic stream
EP1618935A1 (en) * 2004-07-20 2006-01-25 FMC Technologies Italia S.p.A. Evaporator system for fruit and vegetables having a low power consumption and a very low heat damage
US20140158518A1 (en) * 2011-07-21 2014-06-12 Vinnolit Gmbh & Co. Kg Method for concentrating aqueous lye and apparatus suitable therefor
CN104162285A (zh) * 2014-07-31 2014-11-26 河南中原黄金冶炼厂有限责任公司 多效轮换蒸发系统
CN105381620A (zh) * 2015-11-12 2016-03-09 浙江星月药物科技股份有限公司 一种双效浓缩器
EP2969952A4 (en) * 2013-03-14 2016-08-31 Dead Sea Works Ltd PROCESS FOR PRECIPITATION OF CARNALLITE FROM AQUEOUS SOLUTIONS
CN106477796A (zh) * 2016-12-21 2017-03-08 北京燕山翔宇环保工程技术有限公司 脱硫废水处理系统及方法
CN106669210A (zh) * 2016-12-12 2017-05-17 江苏迈安德节能蒸发设备有限公司 含盐有机溶液蒸发回收系统
US10227702B2 (en) * 2014-12-05 2019-03-12 Westlake Vinyl Corporation System and method for purifying depleted brine
US10450239B2 (en) 2016-03-22 2019-10-22 Dead Sea Works Ltd. Spherical fertilizers and process for the production thereof
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US10894749B2 (en) 2017-02-10 2021-01-19 Icl Europe Cooperatief U.A. Polyhalite granulation process
US10988419B2 (en) 2016-10-22 2021-04-27 Dead Sea Works Ltd. Binders for the granulation of fertilizers
CN114288694A (zh) * 2021-12-31 2022-04-08 天津农学院 高纯碳酸锂的闪蒸汽压缩式连续结晶系统及工艺
CN114291825A (zh) * 2021-12-27 2022-04-08 重庆博张智能装备有限公司 一种制备烧碱的工艺生产线及工艺方法
US11306033B2 (en) 2016-12-17 2022-04-19 Dead Sea Works Ltd. Process for the production of potassium sulphate and magnesium sulphate from carnallite and sodium sulphate
WO2022117275A1 (de) * 2020-12-01 2022-06-09 Andreas Wilk Vorrichtung und verfahren zur aufkonzentrierung korrosiver flüssigkeiten
US12017198B2 (en) 2018-02-27 2024-06-25 Dead Sea Works Ltd. Potash dust granulation process

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DE2219340C3 (de) * 1972-04-20 1981-05-07 Kali Und Salz Ag, 3500 Kassel Verfahren zur getrennten Gewinnung von verschiedenen Kristallisaten mit stark unterschiedlichen Löslichkeits-Temperatur-Koeffizienten aus gemeinsamen, Krustenbildner enthaltenden Lösungen
US4953607A (en) * 1989-02-17 1990-09-04 A. Ahlstrom Multistage evaporating system
CN104001338B (zh) * 2014-05-13 2018-02-02 上海金力泰化工股份有限公司 一种脱溶剂系统及其操作工艺
CN111359240B (zh) * 2020-03-30 2021-08-20 山东凯斯达机械制造有限公司 一种管式降膜蒸发器、浓缩装置及其使用方法和工艺
CN111467821B (zh) * 2020-06-22 2020-10-02 富海(东营)新材料科技有限公司 砜类材料生产过程中副产物盐的回收装置及工艺
CN114949893B (zh) * 2022-06-01 2024-04-19 启东神农机械有限公司 从盐湖卤水中生产氯化锂的蒸发结晶工艺及装置

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US2330221A (en) * 1937-10-04 1943-09-28 Buffalo Foundry & Machine Co Method and apparatus for concentrating liquids which upon concentration deposit crystals and leave a residual concentrated liquor
US2459302A (en) * 1942-12-10 1949-01-18 American Viscose Corp Concentration of salts having minimum solubilities at temperatures above those of the initial solutions
DE906691C (de) * 1951-01-09 1954-03-18 Metallgesellschaft Ag Verfahren zum Eindampfen von Fluessigkeiten
US2744571A (en) * 1953-09-28 1956-05-08 Goslin Birmingham Mfg Company Evaporating process

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US1799478A (en) * 1925-02-05 1931-04-07 David D Peebles Method of evaporating liquids and apparatus therefor
US1944548A (en) * 1931-07-15 1934-01-23 American Lurgi Corp Process of the separation of solid substances from liquid by vacuum cooling in stages
US2330221A (en) * 1937-10-04 1943-09-28 Buffalo Foundry & Machine Co Method and apparatus for concentrating liquids which upon concentration deposit crystals and leave a residual concentrated liquor
US2459302A (en) * 1942-12-10 1949-01-18 American Viscose Corp Concentration of salts having minimum solubilities at temperatures above those of the initial solutions
DE906691C (de) * 1951-01-09 1954-03-18 Metallgesellschaft Ag Verfahren zum Eindampfen von Fluessigkeiten
US2744571A (en) * 1953-09-28 1956-05-08 Goslin Birmingham Mfg Company Evaporating process

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US3738411A (en) * 1969-08-05 1973-06-12 Tatabanyai Szenbanyak Treatment of aluminate digester liquor
US3912578A (en) * 1973-01-22 1975-10-14 United States Steel Corp Apparatus for and a method of purifying waste fluid
US4087253A (en) * 1975-03-28 1978-05-02 Rhone-Poulenc Industries Method of obtaining caustic soda from a sodium chloride liquor containing sulphate ions recovered from an electrolytic cell
FR2384035A1 (fr) * 1977-03-15 1978-10-13 Asahi Glass Co Ltd Procede de concentration d'une solution d'alcali caustique obtenue par electrolyse du type a membrane echangeur d'ion
US4441958A (en) * 1981-01-27 1984-04-10 Giampaolo Teucci Forced-circulation evaporator plant
EP0114974A2 (de) * 1983-01-28 1984-08-08 Hüls Aktiengesellschaft Verfahren zum Zersetzen natronhaltiger Mehrfachsalze
EP0114974A3 (de) * 1983-01-28 1984-09-05 Hüls Aktiengesellschaft Verfahren zum Zersetzen natronhaltiger Mehrfachsalze
US4981555A (en) * 1988-10-12 1991-01-01 Metallgesellschaft Ag Process and apparatus for concentrating a solution
US5209828A (en) * 1991-12-23 1993-05-11 Mobil Oil Corporation System for concentrating a spent caustic stream
EP1618935A1 (en) * 2004-07-20 2006-01-25 FMC Technologies Italia S.p.A. Evaporator system for fruit and vegetables having a low power consumption and a very low heat damage
US20060016208A1 (en) * 2004-07-20 2006-01-26 Fmc Technologies Italia S.P.A. Evaporator system for fruit and vegetables having a low power consumption and a very low heat damage
US9849400B2 (en) * 2011-07-21 2017-12-26 Thyssenkrupp Uhde Gmbh Method for concentrating aqueous lye and apparatus suitable therefor
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US10450239B2 (en) 2016-03-22 2019-10-22 Dead Sea Works Ltd. Spherical fertilizers and process for the production thereof
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US11306033B2 (en) 2016-12-17 2022-04-19 Dead Sea Works Ltd. Process for the production of potassium sulphate and magnesium sulphate from carnallite and sodium sulphate
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US10894749B2 (en) 2017-02-10 2021-01-19 Icl Europe Cooperatief U.A. Polyhalite granulation process
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GB1113580A (en) 1968-05-15
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