CA1332842C - Liquid phosphine oxide systems for solvent extraction - Google Patents
Liquid phosphine oxide systems for solvent extractionInfo
- Publication number
- CA1332842C CA1332842C CA 444795 CA444795A CA1332842C CA 1332842 C CA1332842 C CA 1332842C CA 444795 CA444795 CA 444795 CA 444795 A CA444795 A CA 444795A CA 1332842 C CA1332842 C CA 1332842C
- Authority
- CA
- Canada
- Prior art keywords
- oxide
- phosphine
- mixture
- carbon atoms
- phosphine oxides
- 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.)
- Expired - Fee Related
Links
- AUONHKJOIZSQGR-UHFFFAOYSA-N oxophosphane Chemical compound P=O AUONHKJOIZSQGR-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 239000007788 liquid Substances 0.000 title claims description 9
- 238000000638 solvent extraction Methods 0.000 title description 2
- 239000000203 mixture Substances 0.000 claims abstract description 71
- 238000000034 method Methods 0.000 claims abstract description 31
- MPQXHAGKBWFSNV-UHFFFAOYSA-N oxidophosphanium Chemical class [PH3]=O MPQXHAGKBWFSNV-UHFFFAOYSA-N 0.000 claims abstract description 29
- 125000004432 carbon atom Chemical group C* 0.000 claims abstract description 23
- 239000007864 aqueous solution Substances 0.000 claims abstract description 17
- 150000002894 organic compounds Chemical class 0.000 claims abstract description 10
- 230000002378 acidificating effect Effects 0.000 claims abstract description 9
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 57
- ZMBHCYHQLYEYDV-UHFFFAOYSA-N trioctylphosphine oxide Chemical compound CCCCCCCCP(=O)(CCCCCCCC)CCCCCCCC ZMBHCYHQLYEYDV-UHFFFAOYSA-N 0.000 claims description 35
- PPDZLUVUQQGIOJ-UHFFFAOYSA-N 1-dihexylphosphorylhexane Chemical compound CCCCCCP(=O)(CCCCCC)CCCCCC PPDZLUVUQQGIOJ-UHFFFAOYSA-N 0.000 claims description 24
- 230000008018 melting Effects 0.000 claims description 17
- 238000002844 melting Methods 0.000 claims description 17
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 claims description 16
- KWKAKUADMBZCLK-UHFFFAOYSA-N 1-octene Chemical compound CCCCCCC=C KWKAKUADMBZCLK-UHFFFAOYSA-N 0.000 claims description 16
- 150000001875 compounds Chemical class 0.000 claims description 15
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 13
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 claims description 12
- 150000001735 carboxylic acids Chemical class 0.000 claims description 10
- XHRRUIJGMKIISX-UHFFFAOYSA-N 1-dihexylphosphoryloctane Chemical compound CCCCCCCCP(=O)(CCCCCC)CCCCCC XHRRUIJGMKIISX-UHFFFAOYSA-N 0.000 claims description 7
- 125000000217 alkyl group Chemical group 0.000 claims description 7
- MKEFGIKZZDCMQC-UHFFFAOYSA-N 1-[hexyl(octyl)phosphoryl]octane Chemical compound CCCCCCCCP(=O)(CCCCCC)CCCCCCCC MKEFGIKZZDCMQC-UHFFFAOYSA-N 0.000 claims description 6
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 6
- 125000003710 aryl alkyl group Chemical group 0.000 claims description 6
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 claims description 6
- 229910000073 phosphorus hydride Inorganic materials 0.000 claims description 6
- 125000000753 cycloalkyl group Chemical group 0.000 claims description 5
- AFFLGGQVNFXPEV-UHFFFAOYSA-N n-decene Natural products CCCCCCCCC=C AFFLGGQVNFXPEV-UHFFFAOYSA-N 0.000 claims description 5
- 150000002989 phenols Chemical class 0.000 claims description 5
- 125000004051 hexyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 claims description 3
- 125000002347 octyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 claims description 3
- 235000019260 propionic acid Nutrition 0.000 claims 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 claims description 3
- BASAKOUVGYHNRZ-UHFFFAOYSA-N oxido(tridecyl)phosphanium Chemical compound C(CCCCCCCCCCCC)[PH2]=O BASAKOUVGYHNRZ-UHFFFAOYSA-N 0.000 claims description 2
- GYGISEPATDGSPS-UHFFFAOYSA-N 1-didecylphosphoryldecane Chemical compound CCCCCCCCCCP(=O)(CCCCCCCCCC)CCCCCCCCCC GYGISEPATDGSPS-UHFFFAOYSA-N 0.000 claims 1
- 125000002704 decyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 claims 1
- 239000002904 solvent Substances 0.000 description 26
- 239000003085 diluting agent Substances 0.000 description 10
- 238000011084 recovery Methods 0.000 description 10
- 238000000605 extraction Methods 0.000 description 8
- 239000012074 organic phase Substances 0.000 description 7
- 239000008346 aqueous phase Substances 0.000 description 6
- 239000012467 final product Substances 0.000 description 6
- 239000000243 solution Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 4
- -1 l-naphthol Chemical compound 0.000 description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 4
- 239000002440 industrial waste Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- NKTOLZVEWDHZMU-UHFFFAOYSA-N 2,5-xylenol Chemical compound CC1=CC=C(C)C(O)=C1 NKTOLZVEWDHZMU-UHFFFAOYSA-N 0.000 description 2
- JWAZRIHNYRIHIV-UHFFFAOYSA-N 2-naphthol Chemical compound C1=CC=CC2=CC(O)=CC=C21 JWAZRIHNYRIHIV-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 239000004305 biphenyl Substances 0.000 description 2
- 235000010290 biphenyl Nutrition 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 230000007257 malfunction Effects 0.000 description 2
- IWDCLRJOBJJRNH-UHFFFAOYSA-N p-cresol Chemical compound CC1=CC=C(O)C=C1 IWDCLRJOBJJRNH-UHFFFAOYSA-N 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N phenylbenzene Natural products C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 description 2
- WQGWDDDVZFFDIG-UHFFFAOYSA-N pyrogallol Chemical compound OC1=CC=CC(O)=C1O WQGWDDDVZFFDIG-UHFFFAOYSA-N 0.000 description 2
- GHMLBKRAJCXXBS-UHFFFAOYSA-N resorcinol Chemical compound OC1=CC=CC(O)=C1 GHMLBKRAJCXXBS-UHFFFAOYSA-N 0.000 description 2
- 208000028292 transient congenital hypothyroidism Diseases 0.000 description 2
- XNKICCFGYSXSAI-UHFFFAOYSA-N 1,1-diphenylpropan-2-amine Chemical compound C=1C=CC=CC=1C(C(N)C)C1=CC=CC=C1 XNKICCFGYSXSAI-UHFFFAOYSA-N 0.000 description 1
- QIGBRXMKCJKVMJ-UHFFFAOYSA-N 1,4-Benzenediol Natural products OC1=CC=C(O)C=C1 QIGBRXMKCJKVMJ-UHFFFAOYSA-N 0.000 description 1
- WWYUQXYAGXKBNE-UHFFFAOYSA-N 1-[bis(2,4,4-trimethylpentyl)phosphoryl]-2,4,4-trimethylpentane Chemical compound CC(C)(C)CC(C)CP(=O)(CC(C)CC(C)(C)C)CC(C)CC(C)(C)C WWYUQXYAGXKBNE-UHFFFAOYSA-N 0.000 description 1
- INLDOHCRAQBZHR-UHFFFAOYSA-N 1-[decyl(hexyl)phosphoryl]decane Chemical compound CCCCCCCCCCP(=O)(CCCCCC)CCCCCCCCCC INLDOHCRAQBZHR-UHFFFAOYSA-N 0.000 description 1
- FTKKDUVZLDDBEN-UHFFFAOYSA-N 1-[ethyl(octyl)phosphoryl]octane Chemical compound CCCCCCCCP(=O)(CC)CCCCCCCC FTKKDUVZLDDBEN-UHFFFAOYSA-N 0.000 description 1
- MSKVTMZQUUEALA-UHFFFAOYSA-N 1-[hexyl(2-methylpropyl)phosphoryl]hexane Chemical compound CCCCCCP(=O)(CC(C)C)CCCCCC MSKVTMZQUUEALA-UHFFFAOYSA-N 0.000 description 1
- BRLCBJSJAACAFG-UHFFFAOYSA-N 1-didodecylphosphoryldodecane Chemical compound CCCCCCCCCCCCP(=O)(CCCCCCCCCCCC)CCCCCCCCCCCC BRLCBJSJAACAFG-UHFFFAOYSA-N 0.000 description 1
- XHOHEJRYAPSRPZ-UHFFFAOYSA-N 1-dioctadecylphosphoryloctadecane Chemical compound CCCCCCCCCCCCCCCCCCP(=O)(CCCCCCCCCCCCCCCCCC)CCCCCCCCCCCCCCCCCC XHOHEJRYAPSRPZ-UHFFFAOYSA-N 0.000 description 1
- IYBQDXWLVISPTB-UHFFFAOYSA-N 1-dioctylphosphoryldecane Chemical compound CCCCCCCCCCP(=O)(CCCCCCCC)CCCCCCCC IYBQDXWLVISPTB-UHFFFAOYSA-N 0.000 description 1
- QWBBPBRQALCEIZ-UHFFFAOYSA-N 2,3-dimethylphenol Chemical compound CC1=CC=CC(O)=C1C QWBBPBRQALCEIZ-UHFFFAOYSA-N 0.000 description 1
- KUFFULVDNCHOFZ-UHFFFAOYSA-N 2,4-xylenol Chemical compound CC1=CC=C(O)C(C)=C1 KUFFULVDNCHOFZ-UHFFFAOYSA-N 0.000 description 1
- PUAQLLVFLMYYJJ-UHFFFAOYSA-N 2-aminopropiophenone Chemical compound CC(N)C(=O)C1=CC=CC=C1 PUAQLLVFLMYYJJ-UHFFFAOYSA-N 0.000 description 1
- KXGFMDJXCMQABM-UHFFFAOYSA-N 2-methoxy-6-methylphenol Chemical compound [CH]OC1=CC=CC([CH])=C1O KXGFMDJXCMQABM-UHFFFAOYSA-N 0.000 description 1
- RKJGHINMWRVRJW-UHFFFAOYSA-N 3-[bis(2-ethylhexyl)phosphorylmethyl]heptane Chemical compound CCCCC(CC)CP(=O)(CC(CC)CCCC)CC(CC)CCCC RKJGHINMWRVRJW-UHFFFAOYSA-N 0.000 description 1
- ORAORDAXVMRVIX-UHFFFAOYSA-N 9-octyl-9$l^{5}-phosphabicyclo[3.3.1]nonane 9-oxide Chemical compound C1CCC2CCCC1P2(=O)CCCCCCCC ORAORDAXVMRVIX-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 125000003545 alkoxy group Chemical group 0.000 description 1
- 229940058344 antitrematodals organophosphorous compound Drugs 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid group Chemical group C(C1=CC=CC=C1)(=O)O WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 1
- 229950011260 betanaphthol Drugs 0.000 description 1
- 229910002056 binary alloy Inorganic materials 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 125000004093 cyano group Chemical group *C#N 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- RDLZJCXTAYHYHX-UHFFFAOYSA-N dibenzylphosphorylmethylbenzene Chemical compound C=1C=CC=CC=1CP(CC=1C=CC=CC=1)(=O)CC1=CC=CC=C1 RDLZJCXTAYHYHX-UHFFFAOYSA-N 0.000 description 1
- LEFPWWWXFFNJAA-UHFFFAOYSA-N dicyclohexylphosphorylcyclohexane Chemical compound C1CCCCC1P(C1CCCCC1)(=O)C1CCCCC1 LEFPWWWXFFNJAA-UHFFFAOYSA-N 0.000 description 1
- AOAUYBZIBQRSBZ-UHFFFAOYSA-N dihexylphosphorylmethylbenzene Chemical compound CCCCCCP(=O)(CCCCCC)CC1=CC=CC=C1 AOAUYBZIBQRSBZ-UHFFFAOYSA-N 0.000 description 1
- SZAQMRYDICITOU-UHFFFAOYSA-N dioctylphosphorylmethylbenzene Chemical compound CCCCCCCCP(=O)(CCCCCCCC)CC1=CC=CC=C1 SZAQMRYDICITOU-UHFFFAOYSA-N 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- FUZZWVXGSFPDMH-UHFFFAOYSA-N hexanoic acid group Chemical group C(CCCCC)(=O)O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 description 1
- KXFFIPSYXWNHBC-UHFFFAOYSA-N hexyl(dioctyl)phosphane Chemical compound CCCCCCCCP(CCCCCC)CCCCCCCC KXFFIPSYXWNHBC-UHFFFAOYSA-N 0.000 description 1
- 125000000687 hydroquinonyl group Chemical class C1(O)=C(C=C(O)C=C1)* 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003295 industrial effluent Substances 0.000 description 1
- 150000002484 inorganic compounds Chemical class 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 150000002689 maleic acids Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005007 materials handling Methods 0.000 description 1
- 150000002903 organophosphorus compounds Chemical class 0.000 description 1
- NQPDZGIKBAWPEJ-UHFFFAOYSA-N pentanoic acid group Chemical class C(CCCC)(=O)O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 description 1
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 1
- 239000005011 phenolic resin Substances 0.000 description 1
- 229920001568 phenolic resin Polymers 0.000 description 1
- 150000003003 phosphines Chemical group 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 229940079877 pyrogallol Drugs 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/26—Treatment of water, waste water, or sewage by extraction
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
- C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
- C07F9/02—Phosphorus compounds
- C07F9/28—Phosphorus compounds with one or more P—C bonds
- C07F9/50—Organo-phosphines
- C07F9/53—Organo-phosphine oxides; Organo-phosphine thioxides
- C07F9/5304—Acyclic saturated phosphine oxides or thioxides
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Engineering & Computer Science (AREA)
- Hydrology & Water Resources (AREA)
- Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
A process for the removal of difficult-to-remove acidic organic compounds from aqueous solutions using novel phosphine oxide mixtures in which mixtures at least four phosphine oxides are present, the total number of carbon atoms in an oxide having the lowest no. of C atoms being at least 15, said phosphine oxides being present in an amount of at least 1% by weight and not more than 60% by weight.
Unexpectedly high extractability is achieved using the mixtures.
Unexpectedly high extractability is achieved using the mixtures.
Description
-The present invention relates to the removal of acidic organic compounds from aqueous solution and in particular to the use of phosphine oxide mixtures of four or more such oxides without the use of a diluent for the removal of lower carboxylic acids and phenolic compounds from commercial effluent.
The treatment of aqueous effluent for removal of contami-nants and also the recovery of valuable compounds from solution is a most essential part of modern chemical plants. A number of pro-cedures are used such as steam-stripping and the somewhat more complicated solvent extraction, the latter technique being largely dependent upon the properties of the compounds to be recovered.
The choice of solvent is critical and solvent loss must be mini-mized.
Some organic compounds such as acetic acid and phenol in dilute aqueous solutions are particularly difficult to remove. It is known to extract acetic acid using esters or ketones as solvent.
However, the equilibrium distribution coefficient, K~ (weight fraction of solute in solvent phase/weight fraction in aqueous phase, at equilibrium) for acetic acid with these solvents is about 1.0 or less. This low KD necessitates relatively high solvent flow rates in the extraction process and recovery with these solvents is not economically attractive when there is less than 3 to 5 wt~
of acid in the aqueous solution.
Alternative, and somewhat improved solvent systems have been obtained by the use of certain organophosphorous compounds and in particular phosphine oxides in a diluent. These extractant/
diluent systems are disadvantageous, however, since the presence of _ i _ ~`
~.~
-a diluent (which is often necessary in order that higher melting point extractants can be used) effectively reduces the concentra-tion of extractant and also hinders subsequent stripping operations by volatilizing concurrently with the compound which has been removed from aqueous solution.
The use of 100% extractant as solvent without the use of a diluent is therefore desirable but is limited by the melting point of the extractant and the economic operating temperatures at which removal is conducted. In particular the use of neat tri-alkylphosphine oxides is known but their relatively high meltingpoints require that the removal operation be carried out at above ambient temperatures thus incurring the risk of freeze up during plant malfunction.
It has now been unexpectedly discovered that by use of trialkylphosphine oxides mixtures, not only is the melting point at a more acceptable level but that the ability of the mixture to extract acidic organic compounds from dilute aqueous solutions is high. The mixtures provide unexpectedly high extraction coeffi-cients for weakly extracted compounds such as acetic acid. The organic phase with removed compound can be stripped using several methods such as distillation or stripping with an alkali solution.
Thus, according to the present invention, there is provided a process for removing an acidic organic compound selected from the group consisting of a substituted or unsubstituted car-boxylic acid having one to five carbon atoms and a substituted or unsubstituted phenolic compound from a dilute aqueous solution which comprises contacting said aqueous solution with a mixture of at least four phosphine oxides, having the formulae: R3PO, R3PO, R2R' PO, RR2PO
wherein R and R' are individually selected from the group consisting of alkyl, cycloalkyl, aralkyl and substituted aralkyl, each having C4 - C18, and the total number of carbon atoms in each phosphine oxide is at least 15 and preferably at least 18, said phosphine oxides being present in an amount of at least 1% by weight and not more than 60% by weight.
Preferably, the total number of carbon atoms in a second phosphine oxide having the second lowest number of carbon atoms is at least 20 when the total number of carbon atoms in a first phosphine oxide having the lowest number of carbon atoms is 18, the difference in the total number of carbon atoms between the first oxide and the oxide with the highest number of carbon atoms being at least 6.
More preferably at least one phosphine oxide is present in amount of between about 35-50 wt% and said mixtures of phosphine oxides have a melting point below about 20C, more usually below about 10C.
While the mixtures of the present invention are believed to be useful with a variety of valuable pollutants or impurities in dilute aqueous streams, it is particularly useful for acidic organic compounds such as carboxylic acids and phenolic compounds.
In particular the process is used for removing carboxylic acids having one to five carbon atoms, preferably acetic, propionic, butyric and valeric acids (commonly found in industrial effluents) and also phenol. The carboxylic acids may be substituted by one or more halogen, hydroxyl, cyano or alkoxyl groups. Other specific 1 33284~
-acids which may be removed by the process of the present invention are exemplified by hexanoic, heptanedoic, octanoic, nonanoic, benzoic, succinic, oxalic, malic, lactic, cyanoacetic, glycolic, and maleic acids. Phenolic compounds subject to the instant invention include those substituted by one or more alkyl groups.
Examples of phenoIic compounds which can be removed from dilute aqueous streams include p-cresol, resorcinol, l-naphthol, 2-naph-thol, o-, m- and p-xylenol and unsubstituted or substituted hydroquinone, fluoroglucinol and pyrogallol.
The compound or compounds removed from dilute aqueous solution can be present in any low or moderately low amount in the dilute solution, although usually in an amount less than 5wt% and more likely less than 2wt~ or even lwt~.
The process of the present invention is particularly useful for the recovery of carboxylic acids from paper mill and synthetic fuel oil plants effluents. The process is also valuable for the recovery of phenol from phenolic resin production effluent and in coal gasification. It is believed that the recovery of organic and inorganic compounds which are only normally weakly extractable (e.g. Sb, As, Bi compounds) can be carried out by the process of the present invention.
In the phosphine oxides, when one or more R groups are alkyl, preferred alkyls include about C4 to about C18 and more preferably C6 to C10, straight and branched chain alkyls while preferred cycloalkyls include six carbon to eight carbon substituted or unsubstituted cycloalkyls.
-Examples of suitable phosphine oxides include, but are not limited to, tri-n-hexylphosphine oxide (THPO), tri-n-octyl-phosphine oxide (TOPO), tris(2,4,4-trimethylpentyl)-phosphine oxide, tricyclohexylphosphine oxide, tri-n-dodecylphosphine oxide, tri-n-octadecylphosphine oxide, tris(2-ethylhexyl)phosphine oxide, di-n-octylethylphosphine oxide, di-n-hexylisobutylphosphine oxide, octyldiisobutylphosphine oxide, tribenzylphosphine oxide, di-n-hexylbenzylphosphine oxide, di-n-octylbenzylphosphine oxide, 9-octyl-9-phosphabicyclo[3.3.1]nonane-9-oxide, dihexylmono-octylphosphine oxide, dioctylmonohexylphosphine oxide,dihexylmonodecylphosphine oxide, didecylmonohexylphosphine oxide, dioctylmonodecylphosphine oxide, didecylmonooctylphosphine oxide, and dihecylmonobutylphosphine oxide.
While all oxides should be present in an amount of at least lwt% and not more than 60wt%, a preferred amount for at least one said oxide is between about 1.5-10.0 wt%. Although more than four phosphine oxides can be used in the mixture, it is most convenient to produce a quaternary mix from two olefinic compounds. A particularly preferred four part mix is tri-n-octyl-phosphine oxide (TOPO) tri-n-hexyl-phosphine oxide (THPO), dihexylmonooctylphosphine oxide and dioctylmonohexyl-phosphine oxide. However a synergistic effect to give unex-pectedly increased KD values may be obtained with four or more part mixes of the above named phosphine oxide.
The phosphine oxides used in the mixture are selected so that the difference in the total number of carbon atoms in at least two of the oxides is at least 2, and may be up to 6 or more.
-i Preferably the melting point of the mixture is belowabout 20C. However, it is desirable that the melting point be still lower in order to improve the efficiency and costs of the process and also provide materials handling advantages.
A melting point of less than about 10C is preferable and thus a phosphine oxide mix melting below about 10C, and more preferably 0C ~ 5C, will from a practical viewpoint be selected for use in the process provided its ability to extract the acidic organic compound is acceptable.
Apart from the energy savings obt~;n~hle by the use of a low melting point phosphine oxide mixture, other advantages of low m.p. mixtures include the avoidance of diluent to be used so that the phosphine oxides can be used neat, and also the avoidance of the possibility of freeze up during plant malfunction. The low m.p. mixture of phosphine oxides also permits, by virtue of depressed m.p., phosphine oxides to be used which previously could only be used at increased temperatures or together with a diluent, the latter use frequently complicating subsequent strip-ping operations.
Additionally, a preferred quaternary phosphine oxide mixture prepared from hexene and octene has only about 20% of THPO as compared with a preferred binary phosphine oxide mixture of THOP/TOPO which has about 70% THOP. Since THPO is more soluble in water than is desirable, the preferred quaternary phosphine oxide mixture with less THPO is clearly less soluble in the aqueous solution from which the acidic oxganic compounds are extracted and thus is advantageous over the binary system.
However, a principal advantage of the phosphine oxide mixtures used in the process of the present invention is the unexpectedly increased extractability provided by such mixtures.
This extractability exceeds that of an equal amount of one phosphine oxide when used alone or even binary phosphine oxide mixtures and thus provides for operational savings in amount of phosphine oxide required to extract a desired solute from dilute aqueous solution and a reduction in the size of the SX and distillative strip plants is possible.
A preferred quaternary phosphine oxide mixtures may be prepared by reacting two or more olefinic compounds, such as pentene, hexene, octene and decene, with phosphine. The intermediate tertiary phosphine product from two olefinic compounds, such as octene and hexene, is oxidised with hydrogen peroxide to provide a four-component, trialkylphosphine oxide mixture i.e. R3PO R'3PO R2R'PO RR'2PO. Depending upon the olefinic compound (octene/hexene) ratio, the mixture may be a liquid at room temperature, e.g. the freezing point of a 70% by weight hexene:30 % by weight octene mix is approximately 0C. For practical, handling reasons, the mixture is liquid at room temperature. For example, a nine part mix obtained from hexene, octene and decene has been found to be particularly convenient and effective.
The present invention will now be described in more detail with reference to the following examples, some relating to binary phosphine oxide mixtures for comparison purposes, the examples being provided by way of illustration only.
-The first four examples show the use of C8/C6 mixes and also a C10/C6 mix in the preparation of quaternary phosphine oxide mixtures.
Example 1 Phosphine was reacted in an autoclave with an olefin mixture composed of 70% by weight octene and 30% by weight hexene.
The intermediate reaction products (tertiary phosphines) were subsequently oxidised with hydrogen peroxide to form the final product containing a mixture of four tertiary phosphine oxides.
The product was analysed and found to contain 3.9% trihexylphosphine oxide, 22.8% dihexylmonooctylphosphine oxide, 45.7% dioctyl-monohexylphosphine oxide and 27.6~ trioctylphosphine oxide (weight basis). The final product was a liquid at room temperature with a melting range of 8 to 17C.
Example 2 Example 1 was repeated using an olefin mixture composed of 60% by weight octene and 40% by weight hexene. The final tertiary phosphine oxide product was analysed and found to contain 8% trihexylphosphine oxide, 31.9% dihexylmonooctylphosphine oxide, 42.8% dioctylmonohexylphosphine oxide and 17.4% trioctylphosphine oxide (weight basis). The final product was a liquid at room temperature with a melting range of minus 5 to 0C.
Example 3 Example 1 was repeated using an olefin mixture composed of 30% by weight octene and 70% by weight hexene. The final product was analysed and found to contain 40.2% trihexylphosphine oxide, 42.6% dihexylmonooctylphosphine oxide, 15.3% dioctyl--monohexylphosphine oxide and 2% trioctylphosphine oxide. The tertiary phosphine oxide mixture was a liquid at room temperature with a melting range of minus 7 to plus 6C.
Example 4 Example 1 was repeated using an olefin mixture composed of 50% by weight decene and 50% by weight hexene. The final product was analysed and found to contain 22% trihexylphosphine oxide, 42.5% dihexylmonodecylphosphine oxide, 28.9% didecyl-monohexylphosphine oxide and 6.4% tridecylphosphine oxide. The final product was a liquid at room temperature with a melting range of minus 5 to plus 10C.
Example 5 Samples of solvent were tested for extractability of acetic acid and also phenol from dilute aqueous solution. Each solvent sample was shaken and mixed with a fixed amount of aqueous solution cont~;n;~g acetic acid. After several minutes the aqueous phase and organic phase were allowed to separate and the aqueous phase analysed for acetic acid presence. The procedure was repeated with the aqueous phase until all acetic acid had been recovered and passed into the organic phase. The amount, by volume, of organic phase (solvent) required for 100% recovery is indicated by the aqueous/organic (A/O) ratio.
Acetic Acid (Commercial Effluent) A/O for Sample Solvent 100% Recovery 1 150 gpl TOPO in DPA 0.5 2 400 gpl TOPO in DPA 0.66 3 THPO/TOPO (65/35 wt% ratio) 2.0 _ g _ Phenol (Synthetic Solution) A/O for Sample Solvent 100% Recovery 1 100 gpl TOPO in Conoco 500 2 2 200 gpl TOPO in Conoco 500 3 3 325 gpl TOPO in Conoco 500 5 4 THPO/TOPO (65/35 wt% ratio) 10 Thus in samples 1 and 2, TOPO was dissolved in D.P.A., a commercial diluent supplied by Conoco which is formed of diphenyl alkanes, and it can be seen that an increased amount of TOPO in the solvent requires less organic phase to be used, i.e. the aqueous/ organic (A/O) ratio is increased. However, in solvent sample 3, the phosphine oxide mixture (65 wt% : 35 wt% of THPO:TOPO) gives substantially increased ability to extract the acetic acid. Also, in the phenol extraction, sample 4 gives a substantially increased A/O value thereby clearly indicating that less organic (solvent) phase is necessary for 100% recovery of phenol from the aqueous solution.
Example 6 An aqueous commercial waste effluent containing acetic and propionic acid in an amount of 6.15 and 1.50 gpl was extracted using a THPO/TOPO mixture. The equilibrium concentration for each of the carboxylic acids was measured for different A/O ratios.
-Table l Carboxylic Acid Extraction from Commercial Waste Effluent which includes Acetic and Propionic Acid Solvent (wt%) : 65 THPO, 35 TOPO
Temperature : 50C
Equilibrium Concen*ra~tion (gpl)*
Acetic Propionic A/O Org. Aq. KD Org. Aq. KD
518.3 2.50 7.3 6.15 0.27 22.8 29.70 1.30 7.5 2.78 0.11 25.3 15.54 0.61 9.1 1.47 0.03 49.0 *Based on aqueous analysis and mass balance.
Isotherms for remaining acids in co-incidence with the Y axis.
Additionally, the same effluent was extracted using solvent containing different concentrations of TOPO.
Table 2 Carboxylic Acid Extraction from Commercial Waste Effluent Using 150 and 400 gpl TOPO Solvents Temperature : 50C
Diluent : DPA
Equilibrium Concentration (gpl)*
Acetic Propionic Solvent A/O Org.Aq. KD Org. Aq. KD
150 gpl TOPO 2 3.904.20 0.9 1.80 0.60 3.0 in DPA 1 3.452.70 1.3 1.15 0.35 3.3 400 gpl TOPO 2 5.102.60 2.0 2.53 0.24 10.5 in DPA l 4.701.45 3.2 1.40 0.10 14.0 *Based on aqueous analysis and mass balance.
Isotherms for other acids essentially co-incident with the Y axis It is clearly demonstrated that KD values for the THPO/
TOPO mixture are far in excess of the KD values for the TOPO alone in a diphenyl alkane (DPA) diluent, for corresponding A/O ratios.
Example 7 An aqueous solution containing 10 gpl phenol was extrac-ted with solvents having different extractant concentrations.
Table 3 Phenol Recovery The Effect of Extractant Concentration Solvents : (1) 100 gpl TOPO in Conoco 500 (2) 200 gpl TOPO in Conoco 500 (3) 325 gpl TOPO in Conoco 500 (4) 65 w/o THPO, 35 w/o TOPO
Aqueous : 10 gpl Phenol (nominal) Solution Temperature : 50C
Equilibrium ?henol Conc.(gp ) 100 gpl TOPO 200 gpl TO?O 325 gpl TO O THPO/TOPO
A~O Org- Aq- KD Org.~Aq. KD Org- A~ D Org. Aq. KD
1 10.1 0.10 101 9.84 0.04 246 10.5 0.04 262 9.93 0.02 497 2 19.4 0.47 41 19.6 0.10 196 20.9 0.08 260 19.8 0.03 660 5 34.3 3.34 10 45.0 0.87 52 - - - 49.4 0.07 706 -The equilibrium phenol concentrations in the organic and aqueous phases for various A/O values was determined and the equi-librium distribution coefficient, KD calculated. Again it can be seen that the KD values for the phosphine oxide mixture is unexpec-tedly higher than the single oxide solvents, for all A/O values.
Example 8 The following table 4 illustrates that a preferred quaternary phosphine oxide mixture from 70% by weight hexene and 30% by weight octene (example 3) has improved performance characteristics for use as a solvent extractant when compared with a binary mixture of 65 wt. % THPO/35 wt % TOPO.
Acetic Acid Extraction Isotherms Comparing Binary and Quaternary Phosphine Oxide Mixtures Solvents: (1) 70 Hexyl, 30 Octyl Quaternary (2) 65 Hexyl, 35 Octyl Binary Aqueous : 10.25 gpl Acetic Acid (snythetic) Temperature : 50C
Time : 5 mins Equilibrium Acetic Acid Concentration (gpl) 70:30 Quat 65:35 Binary A/O Organic Aqueous KD Organic Aqueous KD
52.7 4.9810.58 47.1 5.54 8.50 32.4 3.788.57 28.0 4.65 6.02 2 16.0 2.257.11 15.5 2.48 6.25 1 8.60 1.575.48 8.85 1.40 6.32 0.5 4.75 0.756.33 4.74 0.78 6.08 Thus, when equilibrium acetic acid concentrations in the organic and aqueous phases for various A/O values are used to calculate the KD values, it can be seen that the KD values for the quaternary mixture is unexpectedly higher than for the binary mixture, particularly at high acetic acid loadings (high A/O
ratios). Furthermore, interpolations from the acetic acid isotherms, given in Table 4, show complete extraction in 4 stages at A/O = 2 for the binary mix. Only 3 stages at A/O = 2 are required when the comparable quaternary is used.
The following graphically illustrates the improved extraction characteristics of the quaternary phosphine oxide mixture of example 8 when compared with the binary mixture.
The treatment of aqueous effluent for removal of contami-nants and also the recovery of valuable compounds from solution is a most essential part of modern chemical plants. A number of pro-cedures are used such as steam-stripping and the somewhat more complicated solvent extraction, the latter technique being largely dependent upon the properties of the compounds to be recovered.
The choice of solvent is critical and solvent loss must be mini-mized.
Some organic compounds such as acetic acid and phenol in dilute aqueous solutions are particularly difficult to remove. It is known to extract acetic acid using esters or ketones as solvent.
However, the equilibrium distribution coefficient, K~ (weight fraction of solute in solvent phase/weight fraction in aqueous phase, at equilibrium) for acetic acid with these solvents is about 1.0 or less. This low KD necessitates relatively high solvent flow rates in the extraction process and recovery with these solvents is not economically attractive when there is less than 3 to 5 wt~
of acid in the aqueous solution.
Alternative, and somewhat improved solvent systems have been obtained by the use of certain organophosphorous compounds and in particular phosphine oxides in a diluent. These extractant/
diluent systems are disadvantageous, however, since the presence of _ i _ ~`
~.~
-a diluent (which is often necessary in order that higher melting point extractants can be used) effectively reduces the concentra-tion of extractant and also hinders subsequent stripping operations by volatilizing concurrently with the compound which has been removed from aqueous solution.
The use of 100% extractant as solvent without the use of a diluent is therefore desirable but is limited by the melting point of the extractant and the economic operating temperatures at which removal is conducted. In particular the use of neat tri-alkylphosphine oxides is known but their relatively high meltingpoints require that the removal operation be carried out at above ambient temperatures thus incurring the risk of freeze up during plant malfunction.
It has now been unexpectedly discovered that by use of trialkylphosphine oxides mixtures, not only is the melting point at a more acceptable level but that the ability of the mixture to extract acidic organic compounds from dilute aqueous solutions is high. The mixtures provide unexpectedly high extraction coeffi-cients for weakly extracted compounds such as acetic acid. The organic phase with removed compound can be stripped using several methods such as distillation or stripping with an alkali solution.
Thus, according to the present invention, there is provided a process for removing an acidic organic compound selected from the group consisting of a substituted or unsubstituted car-boxylic acid having one to five carbon atoms and a substituted or unsubstituted phenolic compound from a dilute aqueous solution which comprises contacting said aqueous solution with a mixture of at least four phosphine oxides, having the formulae: R3PO, R3PO, R2R' PO, RR2PO
wherein R and R' are individually selected from the group consisting of alkyl, cycloalkyl, aralkyl and substituted aralkyl, each having C4 - C18, and the total number of carbon atoms in each phosphine oxide is at least 15 and preferably at least 18, said phosphine oxides being present in an amount of at least 1% by weight and not more than 60% by weight.
Preferably, the total number of carbon atoms in a second phosphine oxide having the second lowest number of carbon atoms is at least 20 when the total number of carbon atoms in a first phosphine oxide having the lowest number of carbon atoms is 18, the difference in the total number of carbon atoms between the first oxide and the oxide with the highest number of carbon atoms being at least 6.
More preferably at least one phosphine oxide is present in amount of between about 35-50 wt% and said mixtures of phosphine oxides have a melting point below about 20C, more usually below about 10C.
While the mixtures of the present invention are believed to be useful with a variety of valuable pollutants or impurities in dilute aqueous streams, it is particularly useful for acidic organic compounds such as carboxylic acids and phenolic compounds.
In particular the process is used for removing carboxylic acids having one to five carbon atoms, preferably acetic, propionic, butyric and valeric acids (commonly found in industrial effluents) and also phenol. The carboxylic acids may be substituted by one or more halogen, hydroxyl, cyano or alkoxyl groups. Other specific 1 33284~
-acids which may be removed by the process of the present invention are exemplified by hexanoic, heptanedoic, octanoic, nonanoic, benzoic, succinic, oxalic, malic, lactic, cyanoacetic, glycolic, and maleic acids. Phenolic compounds subject to the instant invention include those substituted by one or more alkyl groups.
Examples of phenoIic compounds which can be removed from dilute aqueous streams include p-cresol, resorcinol, l-naphthol, 2-naph-thol, o-, m- and p-xylenol and unsubstituted or substituted hydroquinone, fluoroglucinol and pyrogallol.
The compound or compounds removed from dilute aqueous solution can be present in any low or moderately low amount in the dilute solution, although usually in an amount less than 5wt% and more likely less than 2wt~ or even lwt~.
The process of the present invention is particularly useful for the recovery of carboxylic acids from paper mill and synthetic fuel oil plants effluents. The process is also valuable for the recovery of phenol from phenolic resin production effluent and in coal gasification. It is believed that the recovery of organic and inorganic compounds which are only normally weakly extractable (e.g. Sb, As, Bi compounds) can be carried out by the process of the present invention.
In the phosphine oxides, when one or more R groups are alkyl, preferred alkyls include about C4 to about C18 and more preferably C6 to C10, straight and branched chain alkyls while preferred cycloalkyls include six carbon to eight carbon substituted or unsubstituted cycloalkyls.
-Examples of suitable phosphine oxides include, but are not limited to, tri-n-hexylphosphine oxide (THPO), tri-n-octyl-phosphine oxide (TOPO), tris(2,4,4-trimethylpentyl)-phosphine oxide, tricyclohexylphosphine oxide, tri-n-dodecylphosphine oxide, tri-n-octadecylphosphine oxide, tris(2-ethylhexyl)phosphine oxide, di-n-octylethylphosphine oxide, di-n-hexylisobutylphosphine oxide, octyldiisobutylphosphine oxide, tribenzylphosphine oxide, di-n-hexylbenzylphosphine oxide, di-n-octylbenzylphosphine oxide, 9-octyl-9-phosphabicyclo[3.3.1]nonane-9-oxide, dihexylmono-octylphosphine oxide, dioctylmonohexylphosphine oxide,dihexylmonodecylphosphine oxide, didecylmonohexylphosphine oxide, dioctylmonodecylphosphine oxide, didecylmonooctylphosphine oxide, and dihecylmonobutylphosphine oxide.
While all oxides should be present in an amount of at least lwt% and not more than 60wt%, a preferred amount for at least one said oxide is between about 1.5-10.0 wt%. Although more than four phosphine oxides can be used in the mixture, it is most convenient to produce a quaternary mix from two olefinic compounds. A particularly preferred four part mix is tri-n-octyl-phosphine oxide (TOPO) tri-n-hexyl-phosphine oxide (THPO), dihexylmonooctylphosphine oxide and dioctylmonohexyl-phosphine oxide. However a synergistic effect to give unex-pectedly increased KD values may be obtained with four or more part mixes of the above named phosphine oxide.
The phosphine oxides used in the mixture are selected so that the difference in the total number of carbon atoms in at least two of the oxides is at least 2, and may be up to 6 or more.
-i Preferably the melting point of the mixture is belowabout 20C. However, it is desirable that the melting point be still lower in order to improve the efficiency and costs of the process and also provide materials handling advantages.
A melting point of less than about 10C is preferable and thus a phosphine oxide mix melting below about 10C, and more preferably 0C ~ 5C, will from a practical viewpoint be selected for use in the process provided its ability to extract the acidic organic compound is acceptable.
Apart from the energy savings obt~;n~hle by the use of a low melting point phosphine oxide mixture, other advantages of low m.p. mixtures include the avoidance of diluent to be used so that the phosphine oxides can be used neat, and also the avoidance of the possibility of freeze up during plant malfunction. The low m.p. mixture of phosphine oxides also permits, by virtue of depressed m.p., phosphine oxides to be used which previously could only be used at increased temperatures or together with a diluent, the latter use frequently complicating subsequent strip-ping operations.
Additionally, a preferred quaternary phosphine oxide mixture prepared from hexene and octene has only about 20% of THPO as compared with a preferred binary phosphine oxide mixture of THOP/TOPO which has about 70% THOP. Since THPO is more soluble in water than is desirable, the preferred quaternary phosphine oxide mixture with less THPO is clearly less soluble in the aqueous solution from which the acidic oxganic compounds are extracted and thus is advantageous over the binary system.
However, a principal advantage of the phosphine oxide mixtures used in the process of the present invention is the unexpectedly increased extractability provided by such mixtures.
This extractability exceeds that of an equal amount of one phosphine oxide when used alone or even binary phosphine oxide mixtures and thus provides for operational savings in amount of phosphine oxide required to extract a desired solute from dilute aqueous solution and a reduction in the size of the SX and distillative strip plants is possible.
A preferred quaternary phosphine oxide mixtures may be prepared by reacting two or more olefinic compounds, such as pentene, hexene, octene and decene, with phosphine. The intermediate tertiary phosphine product from two olefinic compounds, such as octene and hexene, is oxidised with hydrogen peroxide to provide a four-component, trialkylphosphine oxide mixture i.e. R3PO R'3PO R2R'PO RR'2PO. Depending upon the olefinic compound (octene/hexene) ratio, the mixture may be a liquid at room temperature, e.g. the freezing point of a 70% by weight hexene:30 % by weight octene mix is approximately 0C. For practical, handling reasons, the mixture is liquid at room temperature. For example, a nine part mix obtained from hexene, octene and decene has been found to be particularly convenient and effective.
The present invention will now be described in more detail with reference to the following examples, some relating to binary phosphine oxide mixtures for comparison purposes, the examples being provided by way of illustration only.
-The first four examples show the use of C8/C6 mixes and also a C10/C6 mix in the preparation of quaternary phosphine oxide mixtures.
Example 1 Phosphine was reacted in an autoclave with an olefin mixture composed of 70% by weight octene and 30% by weight hexene.
The intermediate reaction products (tertiary phosphines) were subsequently oxidised with hydrogen peroxide to form the final product containing a mixture of four tertiary phosphine oxides.
The product was analysed and found to contain 3.9% trihexylphosphine oxide, 22.8% dihexylmonooctylphosphine oxide, 45.7% dioctyl-monohexylphosphine oxide and 27.6~ trioctylphosphine oxide (weight basis). The final product was a liquid at room temperature with a melting range of 8 to 17C.
Example 2 Example 1 was repeated using an olefin mixture composed of 60% by weight octene and 40% by weight hexene. The final tertiary phosphine oxide product was analysed and found to contain 8% trihexylphosphine oxide, 31.9% dihexylmonooctylphosphine oxide, 42.8% dioctylmonohexylphosphine oxide and 17.4% trioctylphosphine oxide (weight basis). The final product was a liquid at room temperature with a melting range of minus 5 to 0C.
Example 3 Example 1 was repeated using an olefin mixture composed of 30% by weight octene and 70% by weight hexene. The final product was analysed and found to contain 40.2% trihexylphosphine oxide, 42.6% dihexylmonooctylphosphine oxide, 15.3% dioctyl--monohexylphosphine oxide and 2% trioctylphosphine oxide. The tertiary phosphine oxide mixture was a liquid at room temperature with a melting range of minus 7 to plus 6C.
Example 4 Example 1 was repeated using an olefin mixture composed of 50% by weight decene and 50% by weight hexene. The final product was analysed and found to contain 22% trihexylphosphine oxide, 42.5% dihexylmonodecylphosphine oxide, 28.9% didecyl-monohexylphosphine oxide and 6.4% tridecylphosphine oxide. The final product was a liquid at room temperature with a melting range of minus 5 to plus 10C.
Example 5 Samples of solvent were tested for extractability of acetic acid and also phenol from dilute aqueous solution. Each solvent sample was shaken and mixed with a fixed amount of aqueous solution cont~;n;~g acetic acid. After several minutes the aqueous phase and organic phase were allowed to separate and the aqueous phase analysed for acetic acid presence. The procedure was repeated with the aqueous phase until all acetic acid had been recovered and passed into the organic phase. The amount, by volume, of organic phase (solvent) required for 100% recovery is indicated by the aqueous/organic (A/O) ratio.
Acetic Acid (Commercial Effluent) A/O for Sample Solvent 100% Recovery 1 150 gpl TOPO in DPA 0.5 2 400 gpl TOPO in DPA 0.66 3 THPO/TOPO (65/35 wt% ratio) 2.0 _ g _ Phenol (Synthetic Solution) A/O for Sample Solvent 100% Recovery 1 100 gpl TOPO in Conoco 500 2 2 200 gpl TOPO in Conoco 500 3 3 325 gpl TOPO in Conoco 500 5 4 THPO/TOPO (65/35 wt% ratio) 10 Thus in samples 1 and 2, TOPO was dissolved in D.P.A., a commercial diluent supplied by Conoco which is formed of diphenyl alkanes, and it can be seen that an increased amount of TOPO in the solvent requires less organic phase to be used, i.e. the aqueous/ organic (A/O) ratio is increased. However, in solvent sample 3, the phosphine oxide mixture (65 wt% : 35 wt% of THPO:TOPO) gives substantially increased ability to extract the acetic acid. Also, in the phenol extraction, sample 4 gives a substantially increased A/O value thereby clearly indicating that less organic (solvent) phase is necessary for 100% recovery of phenol from the aqueous solution.
Example 6 An aqueous commercial waste effluent containing acetic and propionic acid in an amount of 6.15 and 1.50 gpl was extracted using a THPO/TOPO mixture. The equilibrium concentration for each of the carboxylic acids was measured for different A/O ratios.
-Table l Carboxylic Acid Extraction from Commercial Waste Effluent which includes Acetic and Propionic Acid Solvent (wt%) : 65 THPO, 35 TOPO
Temperature : 50C
Equilibrium Concen*ra~tion (gpl)*
Acetic Propionic A/O Org. Aq. KD Org. Aq. KD
518.3 2.50 7.3 6.15 0.27 22.8 29.70 1.30 7.5 2.78 0.11 25.3 15.54 0.61 9.1 1.47 0.03 49.0 *Based on aqueous analysis and mass balance.
Isotherms for remaining acids in co-incidence with the Y axis.
Additionally, the same effluent was extracted using solvent containing different concentrations of TOPO.
Table 2 Carboxylic Acid Extraction from Commercial Waste Effluent Using 150 and 400 gpl TOPO Solvents Temperature : 50C
Diluent : DPA
Equilibrium Concentration (gpl)*
Acetic Propionic Solvent A/O Org.Aq. KD Org. Aq. KD
150 gpl TOPO 2 3.904.20 0.9 1.80 0.60 3.0 in DPA 1 3.452.70 1.3 1.15 0.35 3.3 400 gpl TOPO 2 5.102.60 2.0 2.53 0.24 10.5 in DPA l 4.701.45 3.2 1.40 0.10 14.0 *Based on aqueous analysis and mass balance.
Isotherms for other acids essentially co-incident with the Y axis It is clearly demonstrated that KD values for the THPO/
TOPO mixture are far in excess of the KD values for the TOPO alone in a diphenyl alkane (DPA) diluent, for corresponding A/O ratios.
Example 7 An aqueous solution containing 10 gpl phenol was extrac-ted with solvents having different extractant concentrations.
Table 3 Phenol Recovery The Effect of Extractant Concentration Solvents : (1) 100 gpl TOPO in Conoco 500 (2) 200 gpl TOPO in Conoco 500 (3) 325 gpl TOPO in Conoco 500 (4) 65 w/o THPO, 35 w/o TOPO
Aqueous : 10 gpl Phenol (nominal) Solution Temperature : 50C
Equilibrium ?henol Conc.(gp ) 100 gpl TOPO 200 gpl TO?O 325 gpl TO O THPO/TOPO
A~O Org- Aq- KD Org.~Aq. KD Org- A~ D Org. Aq. KD
1 10.1 0.10 101 9.84 0.04 246 10.5 0.04 262 9.93 0.02 497 2 19.4 0.47 41 19.6 0.10 196 20.9 0.08 260 19.8 0.03 660 5 34.3 3.34 10 45.0 0.87 52 - - - 49.4 0.07 706 -The equilibrium phenol concentrations in the organic and aqueous phases for various A/O values was determined and the equi-librium distribution coefficient, KD calculated. Again it can be seen that the KD values for the phosphine oxide mixture is unexpec-tedly higher than the single oxide solvents, for all A/O values.
Example 8 The following table 4 illustrates that a preferred quaternary phosphine oxide mixture from 70% by weight hexene and 30% by weight octene (example 3) has improved performance characteristics for use as a solvent extractant when compared with a binary mixture of 65 wt. % THPO/35 wt % TOPO.
Acetic Acid Extraction Isotherms Comparing Binary and Quaternary Phosphine Oxide Mixtures Solvents: (1) 70 Hexyl, 30 Octyl Quaternary (2) 65 Hexyl, 35 Octyl Binary Aqueous : 10.25 gpl Acetic Acid (snythetic) Temperature : 50C
Time : 5 mins Equilibrium Acetic Acid Concentration (gpl) 70:30 Quat 65:35 Binary A/O Organic Aqueous KD Organic Aqueous KD
52.7 4.9810.58 47.1 5.54 8.50 32.4 3.788.57 28.0 4.65 6.02 2 16.0 2.257.11 15.5 2.48 6.25 1 8.60 1.575.48 8.85 1.40 6.32 0.5 4.75 0.756.33 4.74 0.78 6.08 Thus, when equilibrium acetic acid concentrations in the organic and aqueous phases for various A/O values are used to calculate the KD values, it can be seen that the KD values for the quaternary mixture is unexpectedly higher than for the binary mixture, particularly at high acetic acid loadings (high A/O
ratios). Furthermore, interpolations from the acetic acid isotherms, given in Table 4, show complete extraction in 4 stages at A/O = 2 for the binary mix. Only 3 stages at A/O = 2 are required when the comparable quaternary is used.
The following graphically illustrates the improved extraction characteristics of the quaternary phosphine oxide mixture of example 8 when compared with the binary mixture.
Claims (24)
1. A process for removing an acidic organic compound selected from the group consisting of a substituted or unsubstituted carboxylic acid having one to five carbon atoms and a substituted or unsubstituted phenolic compound from a dilute aqueous solution which comprises contacting said aqueous solution with a mixture which is liquid at room temperature of at least four phosphine oxides having the formulae: R3PO, R3'PO, R2R'PO, RR?PO wherein R and R' are individually selected from the group consisting of alkyl, cycloalkyl, aralkyl and substituted aralkyl, each having C4 - C18, and the total number of carbon atoms in each phosphine oxide is at least 15, said phosphine oxides being present in an amount of at least 1% by weight and not more than 60% by weight.
2. A process according to claim 1 wherein said mixture of phosphine oxides has a melting point below about 20°C.
3. A process according to claim 1 wherein the total number of carbon atoms in a first of said phosphine oxides which has the lowest number of carbon atoms is at least 18 and a second of said phosphine oxides is at least 20, the difference in the total number of carbon atoms in the first oxide and the oxide with the highest number of carbon atoms being at least 6.
4. A process according to claim 1 wherein at least one of said phosphine oxide is present in amount of between about 35-50 wt%.
5. A process according to claim 1 wherein said acidic organic compound is selected from the group consisting of acetic acid, propionic acid and phenol.
6. A process according to claim 1 wherein said mixture of phosphine oxide has a melting point below about 10°C.
7. A process according to claim 1 wherein said mixture of phosphine oxides is tri-n-hexylphosphine oxide, tri-n-octylphosphine oxide, dihexylmonooctylphosphine oxide and dioctylmonohexylphosphine oxide.
8. A process according to claim 1 wherein said mixture of phosphine oxides is tri-n-hexylphosphine oxide, tri-n-decylphosphine oxide, dihexylmonodecylphosphine oxide and didecylmonohexylphosphine oxide.
9. A process according to claim 1 wherein said mixture of phosphine oxides includes at least nine phosphine oxides.
10. A process according to claim 9 wherein hexyl, octyl and decyl groups are present in the mixture.
11. A phosphine oxide mixture of at least four phosphine oxides having the formulae: R3PO, R?PO, R2R?PO, RR?PO wherein R and R' are individually selected from the group consisting of alkyl, cycloalkyl, aralkyl and substituted aralkyl, each having C4-C18, and the total number of carbon atoms in each phosphine oxide is at least 15, said phosphine oxides being present in the mixture in an amount of at least 1% by weight and not more than 60% by weight, said mixture being liquid at room temperature.
12. The phosphine oxide mixture of claim 11 having a melting point below 20°C.
13. The phosphine oxide mixture of claim 11 wherein the total number of carbon atoms in a first of said phosphine oxides which has the lowest number of carbon atoms is at least 18 and a second of said phosphine oxides is at least 20, the difference in the total number of carbon atoms in the first oxide and the oxide with the highest number of carbon atoms being at least 6.
14. The phosphine oxide mixture of claim 11 wherein at least one said phosphine oxide is present in an amount of between about 35-50wt%.
15. The phosphine oxide mixture of claim 11 having a melting point below about 10°C.
16. The phosphine oxide mixture of claim 11 comprising between about 2-45% wt trihexylphosphine oxide, 20-45%wt dihexylmonooctylphosphine oxide, 10-48% wt dioctylmonohexyl-phosphine oxide, and 1-30%wt trioctylphosphine oxide.
17. The phosphine oxide mixture of claim 11 comprising between about 20-24% wt trihexylphosphine oxide, 40-45% wt dihexylmonodecylphosphine oxide, 26-33% wt didecylmonohexylphosphine oxide and 4-9% wt tridecylphosphine oxide.
18. A method of preparing the phosphine oxide mixture of claim 11, which comprises reacting at least two olefinic compounds with phosphine to form an intermediate tertiary phosphine product, oxidising said tertiary phosphine product to provide said phosphine oxide mixture of at least four phosphine oxides.
19. The method of claim 18 wherein said oxidixing is effected by addition of hydrogen peroxide.
20. The method of claim 18 or 19 wherein hexene is reacted with octene.
21. The method of claim 18 or 19 wherein between about 25-65% wt octene is reacted with between about 75-35% wt. hexene.
22. The method of claim 18 or 19 wherein about 55-65%wt octene is reacted with about 35-45%wt hexene.
23. The method of claim 18 or 19 wherein hexene is reacted with decene.
24. The method of claim 18 or 19, wherein hexene, octene and decene are reacted and subsequently oxidised to form nine phosphine oxides in said mixture.
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA 444795 CA1332842C (en) | 1984-01-06 | 1984-01-06 | Liquid phosphine oxide systems for solvent extraction |
AT84108117T ATE33617T1 (en) | 1983-07-21 | 1984-07-11 | LIQUID SYSTEMS OF PHOSPHINE OXIDES FOR SOLVENT EXTRACTION. |
EP84108117A EP0132700B1 (en) | 1983-07-21 | 1984-07-11 | Liquid phosphine oxide systems for solvent extraction |
DE8484108117T DE3470517D1 (en) | 1983-07-21 | 1984-07-11 | Liquid phosphine oxide systems for solvent extraction |
BR8403631A BR8403631A (en) | 1983-07-21 | 1984-07-20 | EXTRACTION PROCESS WITH SOLVENT, MIXING OF PHOSPHINE OXIDE AND PROCESS FOR ITS PREPARATION |
NO842984A NO842984L (en) | 1983-07-21 | 1984-07-20 | PROCEDURE AND MEDICINE FOR AA REMOVE ACID ORGANIC COMPOUNDS FROM Aqueous SOLUTIONS |
YU128984A YU45902B (en) | 1983-07-21 | 1984-07-20 | PROCESS FOR PREPARING A PHOSPHIN OXIDE MIXTURE |
FI842933A FI75498C (en) | 1983-07-21 | 1984-07-20 | Solvent extraction process using phosphine oxide mixtures, phosphine oxide mixtures used in the process and preparation thereof. |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA 444795 CA1332842C (en) | 1984-01-06 | 1984-01-06 | Liquid phosphine oxide systems for solvent extraction |
Publications (1)
Publication Number | Publication Date |
---|---|
CA1332842C true CA1332842C (en) | 1994-11-01 |
Family
ID=4126887
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CA 444795 Expired - Fee Related CA1332842C (en) | 1983-07-21 | 1984-01-06 | Liquid phosphine oxide systems for solvent extraction |
Country Status (1)
Country | Link |
---|---|
CA (1) | CA1332842C (en) |
-
1984
- 1984-01-06 CA CA 444795 patent/CA1332842C/en not_active Expired - Fee Related
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