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EP4355452A2 - Procédé de purification d'un liquide d'extraction - Google Patents

Procédé de purification d'un liquide d'extraction

Info

Publication number
EP4355452A2
EP4355452A2 EP22735109.5A EP22735109A EP4355452A2 EP 4355452 A2 EP4355452 A2 EP 4355452A2 EP 22735109 A EP22735109 A EP 22735109A EP 4355452 A2 EP4355452 A2 EP 4355452A2
Authority
EP
European Patent Office
Prior art keywords
liquid
extraction
distillation
phase
stage
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.)
Pending
Application number
EP22735109.5A
Other languages
German (de)
English (en)
Inventor
Lukas ALMHOFER
Robert BISCHOF
Martin MADERA
Klaus SCHLACKL
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.)
Lenzing AG
Original Assignee
Lenzing AG
Chemiefaser Lenzing AG
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 Lenzing AG, Chemiefaser Lenzing AG filed Critical Lenzing AG
Publication of EP4355452A2 publication Critical patent/EP4355452A2/fr
Pending legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0492—Applications, solvents used
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0488—Flow sheets

Definitions

  • This invention relates to a method for the purification of a depleted organic extraction liquid from a production process, said method comprising the following steps in the given sequence: a. intensive mixing the depleted organic extraction liquid with an amine-containing liquid in a first liquid-liquid extraction step, b. phase separation of the two liquids of step a., c. washing of the organic extraction liquid phase of step b. with an aqueous liquid in a second liquid-liquid extraction step, d. phase separation of the two liquids of step c., and e. recycling of the purified organic extraction liquid into the production process, wherein the enriched amine-containing phase of step b. and the enriched aqueous phase of step d. are purified and recycled into steps a. resp. step c..
  • Extraction is a well-known separation operation for many applications, in particular in the chemical process engineering, pharmaceutical industry etc..
  • Commonly used devices for extraction are among others batch wise single stage extractions and multistage countercurrent continuous processes, e.g. continuous batteries of mixer-settlers, packed columns, stirred columns or centrifugal extractors.
  • EP 36406 A1 discloses a method for extracting solutes like acetic acid, formic acid, optionally furfural and the like from an aqueous solution of hydrolysis products of biomasses, e.g. from the hydrolysis of comminuted wood in a pulp cooking process.
  • aqueous solutions may be the condensates of waste liquors formed during the cooking process.
  • the acetic acid, furfural and the like may be interesting by-products of the pulp production in a biorefinery.
  • the extraction according to EP 36406 A1 uses as a solvent a mixture of
  • the depleted extraction solvent still contains some residues, in particular lipophilic compounds with low vapor pressure, like long-chain fatty acids, resin acids, sterols, lignans, etc.) and condensation products of furan derivatives, so called humins, which would be accumulated during repeated recycling cycles. Due to the long residence time, they may form solid particles that can cause significant fouling in the pipes, heat exchangers and other parts of the plant. This requires frequent cleaning or exchange of such parts and causes high operating costs.
  • a further disadvantage of these unwanted residues is that they may act similar to surfactants and thereby may have a negative effect on the phase separation. In a worst case, they may lead to the formation of emulsions, making phase separation impossible.
  • the problem to be solved consisted in preventing fouling of extraction process equipment caused by residues in the depleted extraction solvent, and in particular in removing the unwanted residues from the depleted extraction solvent and the extraction plant itself in an economic way without creating too much waste material in order to keep cost for disposal as low as possible.
  • a further problem to be solved consisted in improving the economy of the process.
  • the amine-containing liquid favourably is not miscible with the organic extraction liquid.
  • the aqueous liquid may be either recovered water from a distillation or fresh water. In a preferred embodiment of the invention it may be an aqueous phase coming from an evaporation plant as the vapour condensate and contains a small amount of acetic acid, i.e. being slightly acidic. The acidic pH may improve the extraction of the amine.
  • the purification of the enriched amine-containing phase 5 of step b. and the enriched aqueous phase 6 of step d. is done by combining both phases and subjecting them to a fractionated distillation 7 and the residue 8 of the fractionated distillation is removed separately.
  • Some amine may get lost during operation of the process of the invention and has to be replaced by fresh amine.
  • the fresh amine can be introduced at a suitable location within the process; one possible location is an inlet into the pipeline of stream 9.
  • the fractionated distillation is a 2-stage distillation consisting of a conventional distillation column 7 for the first stage and an evaporator 12 for the second stage, wherein the sump 11 of the first stage is further distilled in order to increase the amine recovery rate.
  • the fractionated distillation is a 2-stage distillation consisting of a conventional distillation column 7 for the first stage and an evaporator 12 for the second stage, wherein the sump 11 of the first stage is further distilled in order to increase the amine recovery rate.
  • there may be higher efforts needed for cleaning the devices as the evaporator has to be operated at higher temperatures than the distillation column and therefore more residues will occur there.
  • the evaporator has to be bigger than in the second stage, hence needs more cleaning efforts.
  • the distillation 7 in the first stage is controlled in a way to recover as much amine as possible, but to prevent the residues from coagulation and depositing in the first distillation column 7.
  • the concentrated sump 11 is forwarded to a second distillation stage consisting of a kind of evaporator 12 that is designed to process high-viscosity media and that is easier to clean, i.e. to remove the coagulated residues.
  • a thin WO 2022/175564 3 L0766-WO PCT/EP2022/066278 film evaporator is suitable.
  • the separated residues 8 finally are disposed of, e.g. by incineration.
  • the distillation is a 1 -stage distillation consisting of a conventional distillation column.
  • the sump of the distillation stage is removed, the residues in the sump are coagulated by adding an acid and subsequently separated mechanically and the remaining liquid is deprotonated, in particular by adding calcium hydroxide, and recycled into the extraction process.
  • the acid is sulfuric acid.
  • the calcium sulfate formed during neutralization can be separated mechanically, e.g. by filtration, centrifugation or other suitable operations.
  • this whole distillation step may be replaced by simply coagulating the residues by an acid, however this would require more acid, sufficient to neutralize the whole quantity of amine, as well as more calcium hydroxide for deprotonation.
  • the separated residues finally are disposed of, e.g. by incineration.
  • the distillation is a 1 -stage distillation consisting of a conventional distillation column and the sump of the distillation stage is treated with salts of earth alkali metals (oxides, hydroxides, chlorides, etc.) to precipitate fatty acids and hum in particles.
  • the precipitate may be removed separately, e.g. by filtration, flotation or the like.
  • the amine-containing liquid contains one or more alkanolamines of the group containing N- Methylethanolamine (NMEA), 2-(Dimethylamino)ethan-1-ol (DMAE) and N- Methyldiethanolamine.
  • NMEA N-Methylethanolamine
  • NMEA is especially preferred as it can be recovered very well by the process according to the invention. In particular, it shows the best distillation properties in the process according to the invention.
  • amines are forming azeotropes with water and hence cannot be simply distilled.
  • Such amines may either be converted to the corresponding salts by adding an acid, e.g. H2SO4 before entering the distillation column and later WO 2022/175564 3 L0766-WO PCT/EP2022/066278 can be concentrated in the sump of the distillation column.
  • the concentrated ammonium salt can be converted back to the corresponding free amine via neutralization with a base, e.g. NaOH.
  • the free amine may then be separated from the inorganic salt in a distillation step.
  • azeotropic mixtures of these amines may be concentrated to the desired concentration by membrane separation procedures like reverse osmosis. In both cases the separated amines can then be recovered back into the process of the invention.
  • liquid-liquid extraction steps of step a. (2) and/or step c. (3) are continuous extraction steps.
  • Batch extraction steps are in principle possible as well.
  • continuous extraction is generally preferred. Typical devices for such continuous extraction are packed columns, rotating disc contactors, mixer-settler arrangements, etc..
  • liquid-liquid extraction step of step a. is a discontinuous extraction step and step c. is a continuous extraction step.
  • step a. is done in a stirred vessel.
  • the steps a. to e., and, as the case may be, all steps in between are performed at a temperature of between 50 and 100°C, more preferably between 55 and 90°C.
  • the production process may be a process for obtaining by-products from a biomaterial.
  • the biomaterial is wood.
  • the by-products may be acetic acid, furfural and/or other by-products obtainable from a wood pulp manufacturing process, for example in a so-called “biorefinery”.
  • the invention may be applicable also for other production processes wherein biomasses and hydrophobic solvents with low vapor pressure occur, such as, but not limited to reactive extractions with trioctylamine, deep eutectic solvents or recycling of ionic liquids, e.g. in the manufacture of man-made cellulosic fibers.
  • the production process contains a vapor condensate extraction stage and the organic extraction liquid was used to extract the by-products acetic acid and furfural from the vapor condensate and was subjected to a stripping step to deplete the by-products before being subjected to the purification method according to the invention.
  • the quantity of this partial flow may depend on the content of impurities in the organic extraction liquid and may be smaller if less impurities are contained in the liquid. It may be between 0.1 and 100% (weight/weight) of the total organic extraction liquid coming from the vapour condensate extraction stage. In case of a smaller content of impurities the partial flow may be only between 0.1 and 50% (weight/weight), preferably between 0.1 and 20% (weight/weight) or even more preferred between 0.1 and 5% (weight/weight) in case of a very small impurity content.
  • a second washing of the organic extraction liquid phase of step d. with an aqueous liquid 15 in a third liquid-liquid extraction step 14 and subsequently a phase separation of the two liquids of this second washing step are performed.
  • the aqueous liquid 15 may be either recovered water from a distillation or fresh water.
  • the aqueous liquid 15 may be an aqueous phase coming from an evaporation plant as the vapour condensate and contains a small amount of acetic acid, i.e. being slightly acidic. The acidic pH may improve the extraction of the amine.
  • the enriched aqueous phase 16 of this second washing step may be either combined with the enriched aqueous phase 6 of step d. before distillation 7 or forwarded to a wastewater treatment plant with a treatment stage able to remove the amine.
  • a second washing of the organic extraction liquid phase of step d. with an aqueous liquid 15 in a third liquid- liquid extraction step 14 and subsequently a phase separation of the two liquids of this second washing step are performed.
  • the aqueous liquid 16 may be either recovered water from a distillation or fresh water.
  • the aqueous liquid 15 may be an aqueous phase coming from an evaporation plant as the vapour condensate and contains a small amount of acetic acid, i.e. being slightly acidic.
  • the acidic pH may improve the extraction of the amine.
  • the enriched aqueous phase 16 of this second washing step may be either combined with the enriched aqueous phase 6 of step d. before distillation 7 or forwarded to a wastewater treatment plant with a treatment stage able to remove the amine.
  • the fractionated distillation is a 2- stage distillation consisting of a conventional distillation column 7 for the first stage and an evaporator 12 for the second stage, wherein the sump 11 of the first stage is further distilled in order to increase the amine recovery rate.
  • another possible location for the introduction of fresh amine is the container 13.
  • Example 1 Removal of palmitic acid from a depleted organic extraction liquid a) A depleted organic extraction liquid obtained from a commercial biorefinery containing 52.6%w/w undecane and 32.4%w/w trioctylphosphine oxide was analyzed for palmitic acid (by GC) and solid particles (by gravimetry) and found to contain 22.2 g L ⁇ 1 palmitic acid and 0.49%w/w solid particles. The liquid further contains other extractives, water, acetic acid and other residues. A zeta potential of - 44.0 mV for the solid particles was determined using electrophoretic light scattering (20 °C, 1 mg mL 1 in H2O).
  • Example 1 demonstrates (see also Fig. 5) that increasing the amine concentration and/or increasing the temperature may improve the removal of the unwanted residues like palmitic acid from a depleted organic liquid as e.g. coming from a vapor condensate extraction.
  • Example 2 Removal of the amine from the purified organic extraction liquid a) 150 ml_ of the depleted organic extraction solvent described in example 1 was mixed with 150 mL of an aqueous solution of 357 g L 1 2- (dimethylamino)ethan-l-ol at 60 °C and 200 rpm in a double walled glass apparatus. After 15 minutes the stirring was stopped and the phases were allowed to separate. 5 mL sample were withdrawn from the organic phase and analyzed for 2-(dimethylamino)ethan-1-ol. b) 51 g of the extracted organic phase obtained in step a) was stirred with an equal mass of demineralized water at 60 °C and 200 rpm in a double walled glass apparatus.
  • Example 2 demonstrates (see also Fig. 6) that a slightly acidic washing water may improve the amine removal.
  • Example 3 Purification of a depleted organic extraction liquid a) A depleted organic extraction liquid obtained from a commercial biorefinery consisting of 52.6%w/w undecane and 32.4%w/w trioctylphosphine oxide was analyzed for solid particles (by gravimetry) WO 2022/175564 3 L0766-WO PCT/EP2022/066278 and wood extractives (by GC) and found to contain 0.49%w/w solid particles and 52.6 g L 1 wood extractives.
  • Fig. 7 shows gas chromatograms of the solutions of example 3.
  • Example 3 demonstrates that most of the wood extractives and by the additional washing step nearly all of the amine is removed from the organic extraction liquid.
  • Example 4 Distillation of a 2-(dimethylamino)ethan-1-ol solution loaded with palmitic acid a) To 99.8 g of a 357 g L 1 aqueous solution of 2-(dimethylamino)ethan-1 - ol were added 3.0 g of palmitic acid. The resulting solution was charged to a 250 ml_ round bottom flask connected to a condenser equipped with a thermometer and a receiving flask.
  • Example 4 shows that by the distillation in principle palmitic acid successfully can be removed from the amine in a model system.
  • Example 5 Distillation of a loaded solution of 2-(dimethylamino)ethan-1-ol a) A depleted organic extraction liquid obtained from a commercial biorefinery consisting of 52.6%w/w undecane and 32.4%w/w trioctylphosphine oxide was analyzed for solid particles (by gravimetry) and wood extractives (by GC) and found to contain 0.49%w/w solid particles and 52.6 g L 1 wood extractives.
  • Example 5 demonstrates that by the distillation the unwanted residues in a commercially relevant solution successfully can be removed from an aqueous solution of 2 (dimethylamino) ethan-1-ol.
  • Example 6 Precipitation of impurities from the loaded amine phase usinq
  • H2SO4 a depleted organic extraction liquid obtained from a commercial biorefinery consisting of 52.6%w/w undecane and 32.4%w/w trioctylphosphine oxide was analyzed for solid particles (by gravimetry) and wood extractives (by GC) and found to contain 0.49%w/w solid particles and 52.6 g L 1 wood extractives.
  • Example 6 demonstrates that by adding acid the wood extractives can be removed by precipitation. At pH 2.0 other, presently unidentified compounds precipitated, too.
  • Example 7 Purification of a depleted organic extraction liquid using N- Methylethanolamine a) A depleted organic extraction liquid obtained from a commercial biorefinery consisting of 52.6%w/w undecane and 32.4%w/w trioctylphosphine oxide was analyzed for solid particles (by gravimetry) and wood extractives (by GC) and found to contain 1.00%w/w solid particles and 47.8 g L 1 wood extractives. b) 4743 g of this liquid were stirred with 5964 g of an aqueous solution of 325 g L 1 N-Methylethanolamine at 60 °C and 170 rpm in a double walled glass apparatus. After 15 minutes the stirring was stopped and the phases were allowed to separate c) 1400 g of the loaded amine phase were charged to a 2.5 L round bottom flask and the flask was connected to a rotary evaporator.
  • Example 7 demonstrates that in a single extraction step using N-Methylethanolamine most of the wood extractives and by a single washing step a large amount of amine is removed from the organic extraction liquid. By distilling the loaded aqueous solution from the first extraction, 98.6% of N-Methylethanolamine can be recovered.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Extraction Or Liquid Replacement (AREA)

Abstract

La présente invention concerne un procédé de purification d'un liquide d'extraction organique appauvri issu d'un procédé de production, ledit procédé comprenant les étapes suivantes dans la séquence donnée: a. mélange intensif du liquide d'extraction organique appauvri avec un liquide contenant une amine dans une première étape d'extraction liquide-liquide, b. séparation de phase des deux liquides de l'étape a., c. lavage de la phase liquide d'extraction organique de l'étape b. avec un liquide aqueux dans une seconde étape d'extraction liquide-liquide, d. séparation de phase des deux liquides de l'étape c. et e. recyclage du liquide d'extraction organique purifié dans le processus de production, la phase contenant une amine enrichie de l'étape b. et la phase aqueuse enrichie de l'étape d. étant purifiées et recyclées dans les étapes a. respectivement c.
EP22735109.5A 2021-06-18 2022-06-15 Procédé de purification d'un liquide d'extraction Pending EP4355452A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP21180315.0A EP4104913A1 (fr) 2021-06-18 2021-06-18 Procédé de purification d'un liquide d'extraction
PCT/EP2022/066278 WO2022175564A2 (fr) 2021-06-18 2022-06-15 Procédé de purification d'un liquide d'extraction

Publications (1)

Publication Number Publication Date
EP4355452A2 true EP4355452A2 (fr) 2024-04-24

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EP21180315.0A Withdrawn EP4104913A1 (fr) 2021-06-18 2021-06-18 Procédé de purification d'un liquide d'extraction
EP22735109.5A Pending EP4355452A2 (fr) 2021-06-18 2022-06-15 Procédé de purification d'un liquide d'extraction

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WO (1) WO2022175564A2 (fr)

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Publication number Priority date Publication date Assignee Title
CN118454284A (zh) * 2024-04-30 2024-08-09 云南云蛭康生物科技有限公司 一种高效的菲牛蛭提取物的液膜萃取方法

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT365080B (de) 1980-03-14 1981-12-10 Kanzler Walter Verfahren zur extraktion von essigsaeure, ameisen- saeure, gegebenenfalls furfurol
KR100738507B1 (ko) * 2006-01-24 2007-07-11 대일개발 주식회사 전자산업 에칭과정의 혼합폐산액으로부터 각 산을 분리회수하는 방법
CN101977664B (zh) * 2008-03-20 2014-02-26 塔特和莱利技术有限公司 从叔酰胺溶剂中去除酸
WO2011139830A2 (fr) * 2010-04-29 2011-11-10 University Of Maine System Board Of Trustees Elimination de contaminants d'un solvant d'extraction liquide-liquide
FI126351B (en) * 2011-11-04 2016-10-14 Taminco Finland Oy Method and apparatus for separating at least one carboxylic acid and furfural from a dilute aqueous solution

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Publication number Publication date
WO2022175564A2 (fr) 2022-08-25
EP4104913A1 (fr) 2022-12-21
WO2022175564A3 (fr) 2022-10-20

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