NO148068B - PROCEDURE FOR THE RECOVERY OF CARBOXYL ACIDS FROM Aqueous SOLUTIONS THROUGH EXTRACTION WITH SECONDARY AMIDS AS EXTRACTING AGENTS - Google Patents
PROCEDURE FOR THE RECOVERY OF CARBOXYL ACIDS FROM Aqueous SOLUTIONS THROUGH EXTRACTION WITH SECONDARY AMIDS AS EXTRACTING AGENTS Download PDFInfo
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- NO148068B NO148068B NO763447A NO763447A NO148068B NO 148068 B NO148068 B NO 148068B NO 763447 A NO763447 A NO 763447A NO 763447 A NO763447 A NO 763447A NO 148068 B NO148068 B NO 148068B
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- extraction
- acid
- extractant
- aqueous solutions
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- 239000002253 acid Substances 0.000 title claims description 39
- 238000000605 extraction Methods 0.000 title claims description 31
- 238000000034 method Methods 0.000 title claims description 22
- 239000003795 chemical substances by application Substances 0.000 title claims description 14
- 239000007864 aqueous solution Substances 0.000 title claims description 9
- -1 CARBOXYL ACIDS Chemical class 0.000 title 1
- 238000011084 recovery Methods 0.000 title 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 29
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 claims description 26
- 235000019253 formic acid Nutrition 0.000 claims description 14
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 claims description 13
- 238000004821 distillation Methods 0.000 claims description 7
- 150000001735 carboxylic acids Chemical class 0.000 claims description 6
- 125000003118 aryl group Chemical group 0.000 claims description 5
- 125000004432 carbon atom Chemical group C* 0.000 claims description 5
- 239000000284 extract Substances 0.000 claims description 5
- 150000003334 secondary amides Chemical class 0.000 claims description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 claims description 3
- NZMAJUHVSZBJHL-UHFFFAOYSA-N n,n-dibutylformamide Chemical compound CCCCN(C=O)CCCC NZMAJUHVSZBJHL-UHFFFAOYSA-N 0.000 claims description 3
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 claims description 3
- 125000000217 alkyl group Chemical group 0.000 claims description 2
- 125000003710 aryl alkyl group Chemical group 0.000 claims description 2
- 125000000753 cycloalkyl group Chemical group 0.000 claims description 2
- UZADBXPHDWZTHP-UHFFFAOYSA-N n-butyl-n-ethyloctanamide Chemical compound CCCCCCCC(=O)N(CC)CCCC UZADBXPHDWZTHP-UHFFFAOYSA-N 0.000 claims description 2
- BVYKEGCGRUJWKS-UHFFFAOYSA-N n-butyl-n-cyclohexylacetamide Chemical compound CCCCN(C(C)=O)C1CCCCC1 BVYKEGCGRUJWKS-UHFFFAOYSA-N 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 15
- 239000000203 mixture Substances 0.000 description 8
- 150000007513 acids Chemical class 0.000 description 7
- 150000001408 amides Chemical class 0.000 description 7
- DLFVBJFMPXGRIB-UHFFFAOYSA-N Acetamide Chemical compound CC(N)=O DLFVBJFMPXGRIB-UHFFFAOYSA-N 0.000 description 6
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 6
- 238000009826 distribution Methods 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 235000019260 propionic acid Nutrition 0.000 description 3
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 2
- SYBYTAAJFKOIEJ-UHFFFAOYSA-N 3-Methylbutan-2-one Chemical compound CC(C)C(C)=O SYBYTAAJFKOIEJ-UHFFFAOYSA-N 0.000 description 2
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 2
- ZHNUHDYFZUAESO-UHFFFAOYSA-N Formamide Chemical compound NC=O ZHNUHDYFZUAESO-UHFFFAOYSA-N 0.000 description 2
- OJGMBLNIHDZDGS-UHFFFAOYSA-N N-Ethylaniline Chemical compound CCNC1=CC=CC=C1 OJGMBLNIHDZDGS-UHFFFAOYSA-N 0.000 description 2
- AFBPFSWMIHJQDM-UHFFFAOYSA-N N-methylaniline Chemical compound CNC1=CC=CC=C1 AFBPFSWMIHJQDM-UHFFFAOYSA-N 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000000895 extractive distillation Methods 0.000 description 2
- MLFHJEHSLIIPHL-UHFFFAOYSA-N isoamyl acetate Chemical compound CC(C)CCOC(C)=O MLFHJEHSLIIPHL-UHFFFAOYSA-N 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- CXMXRPHRNRROMY-UHFFFAOYSA-N sebacic acid Chemical compound OC(=O)CCCCCCCCC(O)=O CXMXRPHRNRROMY-UHFFFAOYSA-N 0.000 description 2
- 238000001577 simple distillation Methods 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- SPPWGCYEYAMHDT-UHFFFAOYSA-N 1,4-di(propan-2-yl)benzene Chemical compound CC(C)C1=CC=C(C(C)C)C=C1 SPPWGCYEYAMHDT-UHFFFAOYSA-N 0.000 description 1
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- XBPCUCUWBYBCDP-UHFFFAOYSA-N Dicyclohexylamine Chemical compound C1CCCCC1NC1CCCCC1 XBPCUCUWBYBCDP-UHFFFAOYSA-N 0.000 description 1
- OHLUUHNLEMFGTQ-UHFFFAOYSA-N N-methylacetamide Chemical compound CNC(C)=O OHLUUHNLEMFGTQ-UHFFFAOYSA-N 0.000 description 1
- 235000011054 acetic acid Nutrition 0.000 description 1
- 125000000218 acetic acid group Chemical group C(C)(=O)* 0.000 description 1
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N alpha-methyl toluene Natural products CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 1
- 125000003368 amide group Chemical group 0.000 description 1
- 239000011260 aqueous acid Substances 0.000 description 1
- 239000012736 aqueous medium Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000001588 bifunctional effect Effects 0.000 description 1
- 230000001914 calming effect Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000001944 continuous distillation Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 150000003948 formamides Chemical class 0.000 description 1
- 150000004674 formic acids Chemical class 0.000 description 1
- 229940117955 isoamyl acetate Drugs 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- VXXLEXCQCSPKFI-UHFFFAOYSA-N n-butylcyclohexanamine Chemical compound CCCCNC1CCCCC1 VXXLEXCQCSPKFI-UHFFFAOYSA-N 0.000 description 1
- GSVWUPPSQAZZTF-UHFFFAOYSA-N n-ethyl-n-methylhexan-1-amine Chemical compound CCCCCCN(C)CC GSVWUPPSQAZZTF-UHFFFAOYSA-N 0.000 description 1
- AGVKXDPPPSLISR-UHFFFAOYSA-N n-ethylcyclohexanamine Chemical compound CCNC1CCCCC1 AGVKXDPPPSLISR-UHFFFAOYSA-N 0.000 description 1
- RIWRFSMVIUAEBX-UHFFFAOYSA-N n-methyl-1-phenylmethanamine Chemical compound CNCC1=CC=CC=C1 RIWRFSMVIUAEBX-UHFFFAOYSA-N 0.000 description 1
- BGWFQRDYRSCOCO-UHFFFAOYSA-N n-methylheptan-2-amine Chemical compound CCCCCC(C)NC BGWFQRDYRSCOCO-UHFFFAOYSA-N 0.000 description 1
- JACMPVXHEARCBO-UHFFFAOYSA-N n-pentylpentan-1-amine Chemical compound CCCCCNCCCCC JACMPVXHEARCBO-UHFFFAOYSA-N 0.000 description 1
- PXKCSKRXWAZGFK-UHFFFAOYSA-N n-propylcyclohexanamine Chemical compound CCCNC1CCCCC1 PXKCSKRXWAZGFK-UHFFFAOYSA-N 0.000 description 1
- LYRFLYHAGKPMFH-UHFFFAOYSA-N octadecanamide Chemical compound CCCCCCCCCCCCCCCCCC(N)=O LYRFLYHAGKPMFH-UHFFFAOYSA-N 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000012074 organic phase Substances 0.000 description 1
- QLNJFJADRCOGBJ-UHFFFAOYSA-N propionamide Chemical compound CCC(N)=O QLNJFJADRCOGBJ-UHFFFAOYSA-N 0.000 description 1
- BDHFUVZGWQCTTF-UHFFFAOYSA-N sulfonic acid Chemical compound OS(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-N 0.000 description 1
- 239000000052 vinegar Substances 0.000 description 1
- 235000021419 vinegar Nutrition 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/48—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Extraction Or Liquid Replacement (AREA)
Description
Den foreliggende oppfinnelse angår en ny fremgangsmåte til utvinning av karboksylsyrer med den generelle formel I The present invention relates to a new method for extracting carboxylic acids with the general formula I
hvor R betyr hydrogen eller en metyl-, etyl- .eller vinylgruppe, where R means hydrogen or a methyl, ethyl or vinyl group,
fra vandige løsninger. from aqueous solutions.
Ved en rekke synteser erholdes karboksylsyrene I i In a series of syntheses, the carboxylic acids I i are obtained
form av fortynnede vandige løsninger. Vil man fremstille syrene i ren eller konsentrert form, så møter man som kjent be-tydelige tekniske vanskeligheter. Fjerning av vannet ved destillasjon, hvilket i tilfelle av maursyrer ikke er mulig med tilfredsstillende lave kostnader p.g.a. azeotropdannelse, krever både meget energi og kostbare destillasjonskolonner med tallrike bunner, da separasjonsvirkningen av en enkelt bunn er liten for systemet syre/vann. form of dilute aqueous solutions. If you want to produce the acids in pure or concentrated form, you will, as is well known, encounter significant technical difficulties. Removal of the water by distillation, which in the case of formic acids is not possible with satisfactorily low costs due to azeotrope formation, requires both a lot of energy and expensive distillation columns with numerous bottoms, as the separation effect of a single bottom is small for the acid/water system.
Ved medrivningsdestillasjon med en vannuløselig væske By entrainment distillation with a water-insoluble liquid
så som etylacetat eller benzen lar vannet seg fjerne, til og med hurtigere og med lavere kostnader til utstyr, men energibehovet er da enda høyere enn ved enkel destillasjon. such as ethyl acetate or benzene, the water can be removed, even faster and with lower costs for equipment, but the energy requirement is then even higher than with simple distillation.
Av de samme grunner er også en ekstraksjonsdestillasjon, For the same reasons, an extractive distillation is also
som foreslått i BRD off.skrift 24 08 011 for avvanning av eddik- as proposed in BRD official document 24 08 011 for the dewatering of vinegar
syre ved hjelp av N-metylacetamid, økonomisk sett ufordelaktig. acid using N-methylacetamide, economically disadvantageous.
Fra U.S. patent 2 578 698 er det kjent at organiske From the U.S. patent 2 578 698 it is known that organic
syrer som inneholder minst to karbonatomer i molekylet, kan utvin- acids that contain at least two carbon atoms in the molecule can be extracted
nes fra en vandig løsning av syren ved at oppløsningen bringes i kontakt med et løsningsmiddel bestående av ét dialkylamid av en organisk syre. Ifølge patentets beskrivelse (spalte 3, linjer 40-44 og spalte 4, linjer 10-14) har man imidlertid ifølge paten- nes from an aqueous solution of the acid by bringing the solution into contact with a solvent consisting of one dialkylamide of an organic acid. According to the patent's description (column 3, lines 40-44 and column 4, lines 10-14), however, according to the patent,
tet bare tatt sikte på å anvende amider only aimed at using amides
hvor R 3er syreresten av en langkjedet karboksylsyre eller en aromatisk sulfonsyre. Videre nevner patentskriftet et amid av . en"bifunksjonell karboksylsyre (sebacinsyre). Ved fremgangsmåten ifølge foreliggende oppfinnelse dreier det seg derimot utelukkende om anvendelse av visse amider av maursyre, eddiksyre, propionsyre og akrylsyre, hvilke ikke er nevnt i U.S. patent 2 578 698* Disse amider er således i det minste å an-se som et utvalg som innebærer nyhet og fordeler sammenlignet med det som er kjent fra det nevnte patent. Da de amider som anvendes ved fremgangsmåten ifølge foreliggende oppfinnelse, er avledet fra de enkleste syrer, medfører fremgangsmåten.vesentlige fordeler, idet et acetamid er betydelig billigere enn eksempelvis et stearyl-amid. Det forslag å anvénde amider av de enkleste syrer er ikke nærliggende på basis av det som er kjent fra U.S.-patent 2 578 698, snarere tvert imot. Det er da også gått en mannsalder siden oven-nevnte patent ble publisert uten at andre i mellomtiden har kommet frem til fremgangsmåten ifølge foreliggende oppfinnelse. where R 3 is the acid residue of a long-chain carboxylic acid or an aromatic sulphonic acid. Furthermore, the patent document mentions an amide of . a"bifunctional carboxylic acid (sebacic acid). The method according to the present invention, on the other hand, involves exclusively the use of certain amides of formic acid, acetic acid, propionic acid and acrylic acid, which are not mentioned in U.S. patent 2,578,698* These amides are thus at least to be regarded as a selection that involves novelty and advantages compared to what is known from the aforementioned patent. As the amides used in the method according to the present invention are derived from the simplest acids, the method entails significant advantages, in that an acetamide is significantly cheaper than, for example, a stearyl amide. The proposal to use amides of the simplest acids is not obvious on the basis of what is known from U.S. Patent 2,578,698, quite the contrary. It has also been a lifetime since the above-mentioned patent was published without others having in the meantime arrived at the method according to the present invention.
I tidens løp er det biitt foreslått én lang rekke separa-sjonsmetoder som.er basert på ekstraksjon av syren ved hjelp av et flytende ekstraksjonsmiddel, såsom isoamylacetat eller metyliso-propylketon. ... De- hittil kjente ekstraksjonsmidlers virkningsgrad er • imidlertid-ikke tilfredsstillende, da disse midler tar opp for lite syre og for meget vann. Det erholdes derfor i alle tilfeller blandinger av ekstraksjonsmiddel, syre og vann, hvilke på sin side krever en relativt kostbar viderebehandling, da ingen av disse ekstrak-cjohsmidler muliggjør en enkel destillativ separasjon av de tre In the course of time, a long series of separation methods have been proposed which are based on extraction of the acid using a liquid extraction agent, such as isoamyl acetate or methyl isopropyl ketone. ... The degree of effectiveness of the extraction agents known to date is, however, not satisfactory, as these agents take up too little acid and too much water. Mixtures of extractant, acid and water are therefore obtained in all cases, which in turn require a relatively expensive further treatment, as none of these extractants enable a simple distillation separation of the three
komponenter. components.
Tii grunn for den foreliggende oppfinnelse lå derfor den oppgave å forbedre virknim/scrsden ved ekstraksjon av karboksylsyrene I fra deres fortynnsdo vandige, løsninger ved valg av bedre egnede ekstraks jcnsmidler ,. The basis for the present invention was therefore the task of improving the effectiveness of the extraction of the carboxylic acids I from their dilute aqueous solutions by choosing more suitable extraction agents.
Oppfinnelsen sngnr således en fremgangsmåte til utvinning av karboksylsyrer med tien generelle formel I The invention thus relates to a method for extracting carboxylic acids of the general formula I
hvor betyr hydrogen eller en metyl-, etyl- eller vinylgruppe, ved ekstraksjon fra deres fortynnede vandige løsninger med et sekundært amid som ekstraksjonsmiddel og påfølgende destillasjon av de således erholdte ekstrakter, karakterisert ved at det som ekstraksjonsmiddel anvendes et sekundært amid med den generelle formel II 2 3 hvor R og R betyr alkyl-, cykloalkyl-, aryl- eller aralkylgrup-per eller sammen utgjør en 1,4- eller 1,5-alkylengruppe med i hvert 2 3 tilfelle 1-8 karbonatomer, hvor summen av karbonatomene i R og R utgjør 7-14, og hvor bare en av disse rester er en arylgruppe, og i hvilken R står for en av restene R . Foretrukne utførelsesfor-mer av fremgangsmåten ifølge oppfinnelsen er angitt i krav 2-4. where means hydrogen or a methyl, ethyl or vinyl group, by extraction from their dilute aqueous solutions with a secondary amide as extractant and subsequent distillation of the thus obtained extracts, characterized in that a secondary amide of the general formula II is used as the extractant 2 3 where R and R mean alkyl, cycloalkyl, aryl or aralkyl groups or together constitute a 1,4- or 1,5-alkylene group with in each 2 3 case 1-8 carbon atoms, where the sum of the carbon atoms in R and R is 7-14, and where only one of these residues is an aryl group, and in which R stands for one of the residues R . Preferred embodiments of the method according to the invention are stated in claims 2-4.
Da det med syren I kan finne sted en omamidering, fore-trekkes alltid slike ekstraksjonsmidler hvor R 4 er lik R 1. I samsvar hermed blir maursyre hensiktsmessig ekstrahert med et formamid, eddiksyre med et acetamid, propionsyre med et propion-syreamid og akrylsyre med et akrylsyreamid II, slik at en omamidering ikke kan fastslås. Skal blandinger av forskjellige syrer, f.eks. maursyre og eddiksyre, isoleres, så anvendes fortrinnsvis forbindelser av formamidrekken som de mest effektive representanter innen den definerte klasse. As reamidation can take place with the acid I, such extraction agents are always preferred where R 4 is equal to R 1. In accordance with this, formic acid is suitably extracted with a formamide, acetic acid with an acetamide, propionic acid with a propionic acid amide and acrylic acid with an acrylic acid amide II, so that an omamidation cannot be determined. Should mixtures of different acids, e.g. formic acid and acetic acid, are isolated, then compounds of the formamide series are preferably used as the most effective representatives within the defined class.
Hva amidgrupperingene angår, så er de forbindelser II, eventuelt blandinger derav, som er avledet fra N-etyl-N-cykloheksylamin, N,N-dicykloheksylamin, N-metyl-N-benzylamin, N-metyl-anilin, N-etyianilin, N,N-diamylam.in, N-metyl-N-2-ety lheksylainin, N-n-butyl-N-cykloheksylamin, N-metyl-N-2-heptylamin eller N-pro-pyl-N-cykloheksylamin, spesielt godt egnet. For maursyre har dibutylformamider, herunder særlig di-n-butylformamid, vist seg å være godt egnet, og for eddiksyre har N-n-butyl-N-2-etylheksyl-acetamid og N-n-butyl-N-cykloheksylacetamid vist seg godt egnet. As far as the amide groups are concerned, they are compounds II, possibly mixtures thereof, which are derived from N-ethyl-N-cyclohexylamine, N,N-dicyclohexylamine, N-methyl-N-benzylamine, N-methyl-aniline, N-ethylaniline, N,N-diamylamin, N-methyl-N-2-ethylhexylamine, N-n-butyl-N-cyclohexylamine, N-methyl-N-2-heptylamine or N-propyl-N-cyclohexylamine, particularly suitable . For formic acid, dibutylformamides, including di-n-butylformamide in particular, have proven to be well suited, and for acetic acid, N-n-butyl-N-2-ethylhexyl acetamide and N-n-butyl-N-cyclohexyl acetamide have proven to be well suited.
Amidene II er enten kjent eller lett å fremstille etter kjente metoder. Ligger deres størkningspunkt over ekstraksjons-temperaturen, må det anvendes blandinger av forskjellige ekstraksjonsmidler II eller en blanding av et ekstraksjonsmiddel II med et løsningsmiddel, fortrinnsvis aromatiske hydrokarboner såsom The amides II are either known or easily prepared by known methods. If their solidification point is above the extraction temperature, mixtures of different extractants II or a mixture of an extractant II with a solvent, preferably aromatic hydrocarbons such as
p-diisopropylbenzen som ikke danner noen azeotrop med syrene. p-diisopropylbenzene which does not form an azeotrope with the acids.
Ved denne arbeidsmåte blir virkningsgraden for ekstraksjonsmiddel II riktignok dårligere, men det oppnås likevel tilfredsstillende mange fordeler sammenlignet med kjente metoder, da den løsnings-middelmehgde som normalt er påkrevet for nedsettelsen av størk-ningspunktene, nemlig 10-40 vekt% beregnet på II, er liten. With this method of working, the efficiency of extractant II is admittedly worse, but many satisfactory advantages are still achieved compared to known methods, as the amount of solvent which is normally required for the reduction of the solidification points, namely 10-40% by weight calculated for II, is small.
Et mål på hvor godt egnet ekstraksjonsmidlet er, er fordelingskoeffisienten, som er definert i eksempel 3 og angitt for noen syre/ekstraksjonsmiddel-systemer. Jo mindre denne verdi er, desto høyere vil den nødvendige apparatmessige kostnad for ekstraksjonen være. Ved siden av fordelingskoeffisienten for syren må imidlertid også fordelingskoeffisienten for vannet tas i betraktning, da utvinningen av ren eller konsentrert syre selvsagt vil kunne utføres ved lavere energiforbruk når ekstraksjonsmidlet opptar mindre vann, hvilket fordelaktig er tilfelle for de midler som anvendes i følge oppfinnelsen. A measure of how well suited the extractant is, is the distribution coefficient, which is defined in example 3 and indicated for some acid/extractant systems. The smaller this value is, the higher the necessary equipment cost for the extraction will be. Alongside the distribution coefficient for the acid, however, the distribution coefficient for the water must also be taken into account, as the extraction of pure or concentrated acid will of course be able to be carried out with lower energy consumption when the extraction agent takes up less water, which is advantageously the case for the agents used according to the invention.
Den nødvendige mengde av ekstraksjonsmiddel II avhenger av forskjellige parametere, herunder særlig temperaturen, mengden og konsentrasjonen av syren, antallet av adskillelsestrinn og de øvrige apparatmessige faktorer som har innflytelse på likevektsinnstillingen og dermed oppholdstiden. Hva ekstraksjonsmidlets og syrens art angår, er det ingen prinsipielle forskjeller. The required amount of extractant II depends on various parameters, including in particular the temperature, the amount and concentration of the acid, the number of separation steps and the other apparatus-related factors that have an influence on the equilibrium setting and thus the residence time. As far as the nature of the extractant and the acid are concerned, there are no fundamental differences.
For ekstraksjonen kommer fortrinnsvis temperaturområdet 0-70°C i betraktning. Ved de nedre verdier innen dette område er ekstraksjonsmidlets evne til å oppta syre større enn ved de høyere temperaturer, mens hastigheten for likevektsinnstillingen derimot er lavere. Det økonomisk sett optimale temperaturområde er 20-40°C. For the extraction, the temperature range 0-70°C is preferably taken into account. At the lower values within this range, the extraction agent's ability to absorb acid is greater than at the higher temperatures, while the speed for the equilibrium setting, on the other hand, is lower. The economically optimal temperature range is 20-40°C.
I temperaturområdet 20-40°C er det ved ekstraksjon av In the temperature range 20-40°C, it is by extraction of
1 kg syre påkrevet med 1-10 kg ekstraksjonsmiddel II ved kontakttider på 1-5 min. Når kontakttiden økes, blir disse verdier lavere, og når kontakttiden nedsettes, er de høyere. De angitte kontakttider gjelder for motstrømsekstraksjon som foretrukket utførelsesform, og det i en enkel ekstraksjonskolonne uten andre hjelpemidler så som plater eller bunner, fyllegemer etc, samt under den forutsetning at det lettere ekstraksjonsmiddel utgjør den sammenhengende fase. Ved anvendelse av flertrinns-ekstrak-sjonsapparater, som f.eks. fylte kolonner eller platekolonner med fortrinnsvis 3-6 teoretiske plater, oppnås en høyere virkningsgrad, slik at mengden av ekstraksjonsmiddel kan reduseres ifølge kjente lovmessigheter. 1 kg of acid required with 1-10 kg of extractant II at contact times of 1-5 min. When the contact time is increased, these values become lower, and when the contact time is decreased, they are higher. The specified contact times apply to countercurrent extraction as the preferred embodiment, and that in a simple extraction column without other aids such as plates or bottoms, fillers, etc., and under the condition that the lighter extractant forms the continuous phase. When using multi-stage extraction devices, such as e.g. packed columns or plate columns with preferably 3-6 theoretical plates, a higher degree of efficiency is achieved, so that the amount of extractant can be reduced according to known laws.
Ovenstående angivelser gjelder syrekonsentrasjoner på 5-50 vekt-% av den vandige løsning, slik det er mest vanlig i praksis. Uttynningsforholdet er temmelig konstant ved 95-99 vekt-%, dvs. at om man utgår fra en 30%'s løsning, så blir det tilbake 0,1-0,3% syre i det vandige medium, og når en 10%'s løs-ning underkastes ekstraksjon, så blir det tilbake en løsning med 0,05-0,1% syre. I alminnelighet er det mest økonomisk å utføre ekstraksjonen så langt at det erholdes en blanding av ekstraksjonsmidlet og en 10-40 vekt-%'s syre. Fra denne blanding blir så vannet avdestillert og deretter syren i en påfølgende kolonne. Dette kan på kjent måte utføres ved at man fjerner bare en del The above statements apply to acid concentrations of 5-50% by weight of the aqueous solution, as is most common in practice. The dilution ratio is fairly constant at 95-99% by weight, i.e. if you start from a 30% solution, then 0.1-0.3% acid remains in the aqueous medium, and when a 10%' s solution is subjected to extraction, then a solution with 0.05-0.1% acid remains. In general, it is most economical to carry out the extraction so far that a mixture of the extractant and a 10-40% by weight acid is obtained. From this mixture the water is then distilled off and then the acid in a subsequent column. This can be carried out in a known manner by removing only a part
av vannet i den første kolonne, mens resten av vannet avdestil-leres sammen med syren i den annen kolonne. I dette tilfelle erholdes en handelsvanlig konsentrert syre istedenfor ren syre. of the water in the first column, while the rest of the water is distilled off together with the acid in the second column. In this case, a commercial concentrated acid is obtained instead of pure acid.
Ovenstående redegjørelse refererer seg til den i praksis nesten enerådende kontinuerlige fremstilling av karboksylsyrene I. Det vil imidlertid forstås at fremgangsmåten også The above explanation refers to the almost exclusively continuous production of the carboxylic acids I in practice. However, it will be understood that the method also
kan utføres diskontinuerlig hvis dette ønskes, idet de tilsvarende rammebetingelser overholdes. can be carried out discontinuously if desired, as long as the corresponding framework conditions are observed.
For fullstendighets skyld nevnes at det karakteristiske trekk ved fremgangsmåten i følge oppfinnelsen beror på ekstraksjonsmidlets art og ikke i den i og for seg kjente ekstraksjons-teknikk. F.eks. kan fremgangsmåten ifølge oppfinnelsen anvendes ved behandling av avvann hvor det ikke først og fremst gjelder å ut-vinne syren, men heller å rense vannet. Videre er det mulig å anvende de nevnte ekstraksjonsmidler for ekstraksjonsdestillasjon av de vannholdige syrer. For the sake of completeness, it is mentioned that the characteristic feature of the method according to the invention is based on the nature of the extractant and not on the extraction technique known per se. E.g. the method according to the invention can be used in the treatment of waste water where it is not primarily necessary to extract the acid, but rather to purify the water. Furthermore, it is possible to use the aforementioned extractants for extractive distillation of the aqueous acids.
Den foreliggende fremgangsmåte gjør det mulig å oppnå The present method makes it possible to achieve
en betraktelig besparelse av energi og investeringskostnader både ved sammenligning med andre ekstraksjonsmetoder og ved sammenligning med destillasjonsopparbeidelsen. Fremgangsmåten medfører fordeler særlig ved utvinning av ren eller konsentrert maursyre og eddiksyre, samt ved fremstilling av vandige løsninger som inneholder flere av syrene I. a considerable saving of energy and investment costs both when compared with other extraction methods and when compared with the distillation process. The method entails advantages particularly when extracting pure or concentrated formic acid and acetic acid, as well as when producing aqueous solutions containing several of the acids I.
EKSEMPEL 1 EXAMPLE 1
1 kg av en 21 vekt-%'s vandig maursyre, slik denne erholdes ved den tekniske syntese ut fra metanol og karbonmonoksyd, ble pr. time og ved 20-25°C innmatet på toppen av en fylt kolonne, til hvilken det nedenfra ble tilført 0,9 kg di-n-butylformamid pr. time i motstrøm. Ekstraksjonsmidlet var den sammenhengende fase. 1 kg of a 21% by weight aqueous formic acid, as obtained by the technical synthesis from methanol and carbon monoxide, was per hour and at 20-25°C fed on top of a packed column, to which 0.9 kg of di-n-butylformamide was added from below per hour in counter current. The extractant was the continuous phase.
Fra en beroligelsessone i kolonnens øvre ende ble det uttatt 1,2 kg ekstraktfase pr. time inneholdende praktisk talt hele maursyremengden (210 g) og 90 g vann, altså 300 g 70%'s maursyre. Ved enkel kontinuerlig destillasjon i en fylt kolonne ble denne syre skilt fra ekstraksjonsmidlet ved 45°C (kolonnetoppen) og 6 0 Torr. From a calming zone at the upper end of the column, 1.2 kg of extract phase was withdrawn per hour containing practically the entire amount of formic acid (210 g) and 90 g of water, i.e. 300 g of 70% formic acid. By simple continuous distillation in a packed column, this acid was separated from the extractant at 45°C (column top) and 60 Torr.
Ekstraksjonsmidlet, som fremdeles inneholdt spor av maursyre, ble resirkulert fra destillasjonskolonnens bunn til ekstraksjonskolonnen. The extractant, which still contained traces of formic acid, was recycled from the bottom of the distillation column to the extraction column.
For utvinning av ca. 90 vekt-%'s maursyre ble det fra den umiddelbart erholdte ekstraktfase avdestillert 70 g vann pr. time i en fylt kolonne (normaltrykk, sumptemperatur 143°C), hvor-etter den blanding som var igjen i kolonnesumpen, ble destillert ved 60 Torr og 42°C (kolonnetoppen) i en 25 platers klokkebunns-kolonne, hvor den 90%'ige syre erholdtes som destillat. For the extraction of approx. 90% by weight of formic acid, 70 g of water per hour in a packed column (normal pressure, sump temperature 143°C), after which the mixture remaining in the column sump was distilled at 60 Torr and 42°C (column top) in a 25-plate bell-bottom column, where the 90% ige acid was obtained as a distillate.
På analog måte ble det ved hjelp av de to kolonner utvunnet praktisk talt vannfri maursyre fra ekstraktfasen. In an analogous manner, practically anhydrous formic acid was recovered from the extract phase with the help of the two columns.
EKSEMPEL 2 EXAMPLE 2
1 kg av' en 15 vekt-%'s vandig eddiksyre ble pr. time 1 kg of a 15% by weight aqueous acetic acid was per hour
og ved romtemperatur ovenfra tilført en 12 platers hullplate-kolonne, til hvilken det nedenfra ble tilført 0,75 kg N-n-butyl-N-2-etylheksylacetamid pr. time. Fra ekstraktfasen, som praktisk talt inneholdt hele eddiksyremengden og dessuten 4 vekt-% vann, ble det analogt eksempel 1 fremstilt 81 vekt-%'s og vannfri eddiksyre. and at room temperature added from above to a 12-plate perforated plate column, to which 0.75 kg of N-n-butyl-N-2-ethylhexylacetamide per hour. From the extract phase, which practically contained the entire amount of acetic acid and also 4% by weight of water, 81% by weight and anhydrous acetic acid was prepared analogously to example 1.
EKSEMPEL 3 EXAMPLE 3
Da ekstraksjonsmidlenes egnethet i første rekke avhenger av fordelingskoeffisienten As the suitability of the extraction agents primarily depends on the distribution coefficient
c _ syrens konsentrasjon i den organiske fase c _ the concentration of the acid in the organic phase
syrens konsentrasjon i den vandige fase the concentration of the acid in the aqueous phase
ble disse koeffisienter beregnet for de praktiske behov ved den foreliggende fremgangsmåte ved at 100 g av ekstraksjonsmidlet ble sammenrørt med 143 g av en 30 vekt-%'s syre (tilsvarer 100 g vann) ved 25°C inntil likevekt var oppnådd. Koeffisienten C ble så these coefficients were calculated for the practical needs of the present method by mixing 100 g of the extractant with 143 g of a 30% by weight acid (equivalent to 100 g of water) at 25°C until equilibrium was achieved. The coefficient C was then
ut fra syrekonsentrasjonene i den organiske og den vandige fase. based on the acid concentrations in the organic and the aqueous phase.
De^n følgende tabell gir en oversikt over fordelings-koeffisientene for noen ekstraksjonsmidler som anvendes i følge oppfinnelsen, i sammenligning med kjente ekstraksjonsmidler. The following table gives an overview of the distribution coefficients for some extraction agents used according to the invention, in comparison with known extraction agents.
A = Maursyre A = Formic acid
E = Eddiksyre E = Acetic acid
P = Propionsyre P = Propionic acid
Acr = Akrylsyre Acr = Acrylic acid
Claims (4)
Applications Claiming Priority (1)
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DE2545658A DE2545658C2 (en) | 1975-10-11 | 1975-10-11 | Process for the production of carboxylic acids from their aqueous solutions |
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NO763447L NO763447L (en) | 1977-04-13 |
NO148068B true NO148068B (en) | 1983-04-25 |
NO148068C NO148068C (en) | 1983-08-03 |
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NO763447A NO148068C (en) | 1975-10-11 | 1976-10-08 | PROCEDURE FOR THE RECOVERY OF CARBOXYL ACIDS FROM Aqueous SOLUTIONS THROUGH EXTRACTION WITH SECONDARY AMIDS AS EXTRACTING AGENTS |
Country Status (11)
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JP (1) | JPS6016410B2 (en) |
BE (1) | BE847154A (en) |
BR (1) | BR7606734A (en) |
CA (1) | CA1065889A (en) |
DE (1) | DE2545658C2 (en) |
ES (1) | ES452288A1 (en) |
FR (1) | FR2327215A1 (en) |
GB (1) | GB1554172A (en) |
IT (1) | IT1068121B (en) |
NL (1) | NL188405C (en) |
NO (1) | NO148068C (en) |
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DE2853991A1 (en) * | 1978-12-14 | 1980-07-03 | Basf Ag | METHOD FOR DETERMINING WATER-FREE OR MOSTLY WATER-FREE FORMIC ACID |
DE2914671A1 (en) * | 1979-04-11 | 1980-10-23 | Basf Ag | METHOD FOR DETERMINING WATER-FREE OR MOSTLY WATER-FREE FORMIC ACID |
NL8103517A (en) * | 1981-07-24 | 1983-02-16 | Badger Bv | METHOD FOR SEPARATING CARBONIC ACIDS FROM MIXTURES WITH NON-ACIDS BY AN ABSORPTION STRIP TREATMENT. |
DE3411384A1 (en) * | 1984-03-28 | 1985-10-10 | Basf Ag, 6700 Ludwigshafen | METHOD FOR THE EXTRACTION OF WATER-FREE OR MOSTLY WATER-FREE FORMIC ACID BY HYDROLYSIS OF METHYLFORMIAT |
DE3417790A1 (en) * | 1984-05-14 | 1985-11-14 | Basf Ag, 6700 Ludwigshafen | METHOD FOR PRODUCING FORMIC ACID |
DE4023353A1 (en) * | 1990-07-23 | 1992-01-30 | Basf Ag | METHOD FOR OBTAINING CARBONIC ACIDS FROM THEIR AQUEOUS SOLUTIONS |
DE4211141A1 (en) * | 1992-04-03 | 1993-10-07 | Basf Ag | Process for the preparation of formic acid by thermal cleavage of quaternary ammonium formates |
US5728872A (en) * | 1994-06-27 | 1998-03-17 | Lutz Riemenschneider | Stabilized acrylic acid compositions |
DE10002793A1 (en) * | 2000-01-24 | 2001-07-26 | Basf Ag | Production of anhydrous formic acid involves hydrolysis of methyl formate followed by distillation, extraction with amide and further distillations, using the amide also as a foam suppressant in first distillation stage |
DE102008053315A1 (en) | 2008-10-27 | 2010-04-29 | Kiefer, Hans, Dr. | Preparation of tetrahydrofuran, comprises heating 1,4-diacetoxy butane in the presence of a strong acid and excess water to reflux and continuously separating the formed tetrahydrofuran by rectification |
WO2012000964A1 (en) | 2010-06-29 | 2012-01-05 | Basf Se | Method for producing formic acid |
US8901350B2 (en) | 2010-06-29 | 2014-12-02 | Basf Se | Process for the preparation of formic acid |
CN103998409B (en) | 2011-12-20 | 2015-10-07 | 巴斯夫欧洲公司 | Prepare the method for formic acid |
US8889905B2 (en) | 2011-12-20 | 2014-11-18 | Basf Se | Process for preparing formic acid |
US8835683B2 (en) | 2011-12-20 | 2014-09-16 | Basf Se | Process for preparing formic acid |
BR112014012602A2 (en) | 2011-12-20 | 2017-06-20 | Basf Se | process to get formic acid |
US9428438B2 (en) | 2012-11-27 | 2016-08-30 | Basf Se | Process for preparing formic acid |
CN104812731A (en) | 2012-11-27 | 2015-07-29 | 巴斯夫欧洲公司 | Method for producing formic acid |
CN109053421A (en) * | 2018-09-18 | 2018-12-21 | 福建师范大学福清分校 | The device and method of mixed acid waste water during a kind of extraction-partition wall rectification process Carboxylic Acid Fibre is plain |
CN117545734A (en) | 2021-05-14 | 2024-02-09 | 瑞环控股株式会社 | Process for recovering carboxylic acid |
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DE2408011A1 (en) * | 1974-02-20 | 1975-09-04 | Hoechst Ag | METHOD FOR OBTAINING TECHNICALLY PURE ACETIC ACID BY EXTRACTIVE DISTILLATION |
-
1975
- 1975-10-11 DE DE2545658A patent/DE2545658C2/en not_active Expired
-
1976
- 1976-09-29 IT IT27806/76A patent/IT1068121B/en active
- 1976-10-07 CA CA262,961A patent/CA1065889A/en not_active Expired
- 1976-10-07 NL NLAANVRAGE7611111,A patent/NL188405C/en not_active IP Right Cessation
- 1976-10-07 GB GB41693/76A patent/GB1554172A/en not_active Expired
- 1976-10-07 BR BR7606734A patent/BR7606734A/en unknown
- 1976-10-08 NO NO763447A patent/NO148068C/en unknown
- 1976-10-08 FR FR7630284A patent/FR2327215A1/en active Granted
- 1976-10-09 ES ES452288A patent/ES452288A1/en not_active Expired
- 1976-10-11 BE BE171402A patent/BE847154A/en not_active IP Right Cessation
- 1976-10-12 JP JP51121368A patent/JPS6016410B2/en not_active Expired
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JPS6016410B2 (en) | 1985-04-25 |
DE2545658A1 (en) | 1977-04-21 |
NO763447L (en) | 1977-04-13 |
JPS5248614A (en) | 1977-04-18 |
NL188405C (en) | 1992-06-16 |
ES452288A1 (en) | 1978-03-01 |
DE2545658C2 (en) | 1985-12-19 |
NO148068C (en) | 1983-08-03 |
FR2327215A1 (en) | 1977-05-06 |
NL7611111A (en) | 1977-04-13 |
BR7606734A (en) | 1977-11-16 |
BE847154A (en) | 1977-04-12 |
FR2327215B1 (en) | 1980-05-09 |
GB1554172A (en) | 1979-10-17 |
CA1065889A (en) | 1979-11-06 |
IT1068121B (en) | 1985-03-21 |
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