CA2202153A1 - Process for the selective separation of morpholine - Google Patents
Process for the selective separation of morpholineInfo
- Publication number
- CA2202153A1 CA2202153A1 CA 2202153 CA2202153A CA2202153A1 CA 2202153 A1 CA2202153 A1 CA 2202153A1 CA 2202153 CA2202153 CA 2202153 CA 2202153 A CA2202153 A CA 2202153A CA 2202153 A1 CA2202153 A1 CA 2202153A1
- Authority
- CA
- Canada
- Prior art keywords
- morpholine
- methylmorpholine
- oxide
- cation exchanger
- nmmo
- 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.)
- Abandoned
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D295/00—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms
- C07D295/02—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements
- C07D295/023—Preparation; Separation; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D295/00—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms
- C07D295/22—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms with hetero atoms directly attached to ring nitrogen atoms
- C07D295/28—Nitrogen atoms
Abstract
The invention relates to a process for the selective separation of morpholine from an aqueous solution containing morpholine, N-methyl morpholine and N-methyl morpholine-N-oxide, in which (A) a quantity of the aqueous solution is taken through a cation exchanger capable of adsorbing morpholine until said exchanger can carry substantially no more morpholine and an eluate substantially free from morpholine but containing N-methyl morpholine and N-methyl morpholine-N-oxide is obtained, and (B) the cation exchanger charged with morpholine is regenerated and re-used in step (A).
Description
CA 022021~3 1997-04-08 PROCESS FOR SELECTIVE SEPARATION OF MORPHOLINE
The present invention is concerned with a process for the selective separation of morpholine from an aqueous solution cont~;ning morpholine, N-methylmorpholine and N-methylmorpholine-N-oxide. In particular, the present invention is concerned with a process for the regeneration of an aqueous process liquid of the amine-oxide process containing morpholine, N-methylmorpholine and N-methylmorpholine-N-oxide.
For some decades there has been searched for processes for the production of cellulose moulded bodies able to substitute the viscose process, today widely employed. As an alternative which is interesting for its reduced environmental impact among other reasons, it has been found to dissolve cellulose without derivatisation in an organic solvent and extrude from this solution moulded bodies, e.g. fibres, films and other moulded bodies. Fibres thus extruded have received by BISFA
(The International Bureau for the Standardization of man made fibers) the generic name Lyocell. By an organic solvent, BISFA understands a mixture of an organic chemical and water.
It has turned out that as an organic solvent, a mixture of a tertiary amine-oxide and water is particularly appropriate for the production of cellulose moulded bodies. As the amine-oxide, primarily N-methylmorpholine-N-oxide (NMMO) is used.
Other amine-oxides are described e.g. in EP-A - 0 s53 070. A
process for the production of mouldable cellulose solutions is known e.g. from EP-A - 0 356 419. For the purposes of the present specification and the present claims, the production o~ cellulose moulded bodies using tertiary amine-oxides generally is referred to as amine-oxide process.
In EP-A - 0 356 419, an amine-oxide process for the production of spinnable cellulose solutions is described, wherein as a starting material among other substances a suspension of cellulose in liquid, aqueous N-methylmorpholine-N-oxide (NMMO) is used. This process CA 022021~3 1997-04-08 consists in transforming the suspension in a thin-film treatment apparatus in one single step and continuously into a mouldable solution. Finally, the mouldable solution is spun into filaments by a forming tool such as a spinneret and the filaments are passed through a precipitation bath.
In the precipitation bath the cellulose is precipitated. The tertiary amine-oxide is accumulated in the precipitation bath. The precipitation bath may contain up to 30 weight% o~
amine-oxide. For economic reasons of the amine-oxide process it is of vital importance to recover the amine-oxide as completely as possible and reuse it for the production of a mouldable cellulose solution. Thus is is necessary to recover NMMO from the precipitation bath.
A process for the recovery of NMMO from diluted aqueous solutions is known from DD-A - 274 435. According to this process, the aqueous solution is passed over exchanger columns filled with styrene/divinylbenzene copolymer conta;n;ng SO3H groups until it reaches its maximum equimolar exhaustion. Subsequently the NMMO is displaced by equimolar amounts of sodium hydroxide solution and the exchanger columns are regenerated by means of acid.
In addition to the amine-oxide however, the degradation products of the amine-oxide are also accumulated in the precipitation bath. These degradation products may be intensively coloured, thus deteriorating the quality of the cellulose moulded bodies produced. On the other hand, other substances may represent an additional safety risk, since under certain conditions the amine-oxide tends to show highly exothermic decomposition reactions and these decomposition reactions may be induced or accelerated by certain substances. These substances have to be removed from the precipitation bath which is to be regenerated before the NMMO
is concentrated and separated.
CA 022021~3 1997-04-08 After removing these unwanted substances, water is withdrawn from the purified precipitation bath which optionally is combined with other process liquids of the amine-oxide process such as vapour condensates formed during the production of the cellulose solution. This may be carried out for instance by means of evaporation. The residue of this evaporation contains highly concentrated aqueous amine-oxide which is recycled again into the amine-oxide process. The vapours of the evaporation consist mainly of water, wherein considerable amounts of N-methylmorpholine, the main degradation product of NMM0, are also dissolved. Moreover, the vapours contain also NMM0 and morpholine. Typically, the vapours contain up to loo mg of NMMO, 240 mg of N-methylmorpholine and up to 30 mg of morpholine per litre.
Conveniently, these vapours are concentrated, e.g. by means of reverse osmosis. The aqueous solution obtained contains typically up to 4 g of NMMO, up to 10 g of N-methylmorpholine and up to approximately 1 g of morpholine.
From EP-A - 0 402 347 it is known to separate amines from waste waters of cellulose processing by means of a cation exchanger. The cation exchanger carries carboxyl groups as functional groups. Afterwards, the cation exchanger charged with the amines is treated with an aqueous solution of a weak acid having a pKa value of more than 3,0 to eluate the amines. The eluate is regenerated by means of distillation, part of the weak acid being separated from the amines and optionally also recovered. By means of this process, up to 94% of N-methylmorpholine and morpholine in aqueous solutions containing both amines are removed from the waste water. The separated amines are disposed by combustion.
Moreover it is known to separate morpholine, N-methylmorpholine and NMMO together from waste waters by means of a cation exchanger (C. Grilc and N. Zitko, Recovery of Morpholine; Chem. Biochem. Eng. Q. 6 (4), 189-193 (1992)).
CA 022021~3 1997-04-08 EP-A - 0 468 951 describes a process for the separation of amine-oxides from aqueous solutions, particularly waste waters, produced in the cellulose process. According to this known process, the waste waters are contacted with a cation exchanger comprising carboxyl groups as functional groups to charge the cation exchanger with the amine-oxides, whereafter the charged cation exchanger is washed and the amine-oxides are treated with an aqueous solution of a weak acid having a pKa value of more than 3,0 to eluate the amine-oxides. This process also aims at eliminating the amine-oxides completely from the waste waters so as to dispose them in an environmentally friendly way.
In the amine-oxide process however, the NMMO losses should be kept as low as possible. Also, N-methylmorpholine should be oxidized again to NMMO and recovered. Oxidation may be carried out for instance using a peroxidic oxidant.
A process for the preparative production of tertiary amine-oxides by means of oxidation of tertiary amines is known e.g.
from EP-A - 0 092 862. According to this process, the amine-oxide is oxidized under pressure with molecular oxygen in an aqueous solvent, said solvent having a pH value approximately equal or higher than the pKa value of the tertiary amine.
DD-A - 259 863 is concerned with the production of aqueous NMMO solutions by means of oxidation of N-methylmorpholine with H22 and by passing the reaction solution over one or more exchanger columns filled with styrene/divinylbenzene copolymer containing sulphonate groups, as well as by adjusting a pH value of the solution to values ranging from 8 to 5 by addition of phosphoric acid.
In an oxidation it is disadvantageous that morpholine present in the process liquid introduced as a contamination together with the tertiary amines is partially transformed into toxic N-nitrosomorpholine, which is accumulated unwantedly in the CA 022021~3 1997-04-08 NMMO cycle. Additionally, other nitrosoamines are also formed in the oxidation reactions.
Oxidation of N-methylmorpholine with H22 to NMMO is known e.g. from EP-A - 0 254 803. From DE-A - 4 140 259, the production of NMMO by a process wherein the formation of nitrosoamines is restricted by scavenging primary and secondary amines, for instance by means of acid halides, is known. EP-A - 0 320 690 describes the production of-amine-oxides substantially free from nitrosoamines by oxidation with peroxides in the presence of a combination of CO2/ascorbic acid acting as a nitrosoamine inhibitor. From EP-A - 0 401 503, oxidation with H22 in water and a co-solvent, preferably a carboxylic acid ester, is known.
According to FR-A - 8 808 039, oxidation is carried out while adding CO2, and according to US-A - 5,216,154, oxidation to NMMO is carried out in a pure C02 atmosphere.
In the state of the art, the forming of nitrosoamine either is not prohibited, or it is achieved by removing the starting products of the N-nitrosomorpholine or by employing additives to slow down the formation rate of the N-nitrosomorpholine.
Particularly in an amine-oxide process comprising a closed cycle, the addition of various chemicals such as acid halides or ascorbic acid or CO2 to the process causes problems in the purification of the process liquids, since the degradation products introduced together with the added chemicals have to be removed from the process. For many chemicals, it is also necessary to consider safety aspects such as the risk of exothermic reactions. Thus, neither of the described processes is appropriate for the regeneration of process liquids of the amine-oxide process.
Thus it is the object of the present invention to provide a process for the selective separation of morpholine from various process liquids of the amine-oxide process wherein substantially only morpholine is separated and NMMO and N-methylmorpholine will remain in the process liquid.
CA 022021~3 1997-04-08 The process according to the invention for selective separation of morpholine from an aqueous solution cont~in;ng morpholine, N-methylmorpholine and NMMO is characterized by the following steps:
(A) passing the aqueous solution over a cation exchanger capable of adsorbing morpholine in such an amount until it cannot be charged substantially with morpholine any more and an eluate substantially free from morpholine but cont~in;ng N-methylmorpholine and N-methylmorpholine-N-oxide is obtained, and (B) regenerating the cation exchanger charged with morpholine and reusing it in step (A).
The present invention is based upon the finding that a cation exchanger evidently has a higher activity for morpholine than for N-methylmorpholine and NMMO and that due to this higher activity a high yield of N-methylmorpholine and NMMO has already been eluated the moment morpholine starts to break through, thus allowing a distinct separation of the morpholine. In detail, the separation is carried out such that first each of the three components, i.e. morpholine, N-methylmorpholine and NMMO, are adsorbed at the fresh cation exchanger. When the cation exchanger is charged with these three components, NMMO starts to break through, since on the one hand the following NMMO cannot be adsorbed any more and on the other the following morpholine and N-methylmorpholine displace the NMMO already adsorbed. This means that the eluate contains at that point actually only NMMO.
When substantially all the NMMO is displaced at the cation exchanger, N-methylmorpholine also appears in the eluate, being displaced by the following morpholine. At that point, the eluate contains NMMO and N-methylmorpholine. Only when substantially no N-methylmorpholine is adsorbed at the cation exchanger and the capacity of the cation exchanger is exhausted, morpholine starts to break through and the CA 022021~3 1997-04-08 eluation has to be interrupted and the cation exchanger regenerated. This can be done for instance using diluted mineral acids.
The cation exchanger employed in the process according to the invention exhibits preferably carboxyl groups and/or sulphonic acid groups.
A preferred embodiment of the process according to the invention is characterized by the further step of (C) subjecting the eluate obtained in step (A) to an oxidation treatment optionally after water has been removed to oxidize N-methylmorpholine to N-methylmorpholine-N-oxide.
This embodiment of the process according to the invention completely prevents the new formation of the toxic N-nitrosomorpholine, since the eluate contains actually no morpholine. Thus the oxidized eluate contains only the usual reduced basic level of N-nitrosomorpholine which occurs in the amine-oxide process.
Conveniently, oxidation is carried out by means of a peroxidic oxidant. As the peroxidic oxidant, in the process according to the invention preferably H22 is used. The H22 is employed preferably as an aqueous solution having 30-50 weight% of H202. The H22 is best employed in an amount of from 0,8 to 2 mole per mole of N-methylmorpholine.
Another preferred embodiment of the process according to the invention is characterized in that the aqueous solution is exposed to ultraviolet radiation having substantially a wavelength of 254 nm during or subsequently to the oxidation treatment. The ultraviolet radiation is best emitted by a mercury low-pressure lamp.
CA 022021~3 1997-04-08 This embodiment of the process according to the invention is based on the finding that N-nitrosomorpholine can be destroyed by exposure to ultraviolet radiation having an intensity maximum of 254 nm. Therefore, when exposure to ultraviolet radiation is carried out during or subsequently to the oxidation treatment, destruction of the N-nitrosomorpholine present at a basic level will occur, and thus it becomes possible to significantly reduce the basic level of this toxic substance.
It has been shown that it is more advantageous to first separate morpholine by means of the cation exchanger and then proceed to oxidize the eluate, since thus the exposure time to ultraviolet radiation and the exposure intensity necessary to destroy the N-nitrosomorpholine are significantly reduced.
When morpholine is not separated before oxidation, an amount of N-nitrosomorpholine equivalent to the morpholine content will be formed again, requiring a significantly higher exposure time and rate for destruction.
The exposure rate may range e.g. from 200 to 500 mJ/cm2, depending on the design of the lamp and the process conditions, particularly the temperature.
General methods for the quantitative analysis of nitrosoamines which use a W exposure and a subsequent determination of the nitrites formed are known (D.E.G.
Shuker, S.R. Tannenbaum, Anal. Chem., 1983, 55, 2152-2155; M.
Rhighezza, M.H. Murello, A.M. Siouffi, J. Chromat., 1987, 410, 145-155; J.J. Conboy, J.H. Hotchkiss, Analyst, 1989, 114, 155-159; B. Buchele, L. Hoffmann, J. Lang, Fresen.J.Anal.Chem., 1990, 336, 328-333). These analytic methods however do not deal with the destruction of N-nitrosomorpholine.
For exposure according to the invention using a low-pressure lamp, the lamp may be hung into a container containing the process liquid which is to be treated. However the lamp may also be arranged in another way. Moreover, exposure may be carried out for instance during a continuous pumping over of the solution to be exposed in a thin-film W-reactor.
The process according to the invention is particularly appropriate for regeneration of a process liquid from the amine-oxide process.
Another preferred embodiment of the process according to the invention comprises the following steps:
(1) passing the above vapours concentrated for instance by means of reverse osmosis over a cation exchanger capable of selectively adsorbing morpholine and safeguarding that the pH value lies in a range of from 6,0 to 9,0, thereafter (2) combining the eluate obtained from the cation exchanger with purified precipitation bath of the amine-oxide process, said precipitation bath containing 10-30 weight%
of NMMO and (3) treating the eluate combined with the precipitation bath in an evaporation reactor with the peroxidic oxidant to oxidize N-methylmorpholine and to concentrate, obtaining concentrated, aqueous NMMO which is recycled again into the amine-oxide process and vapours which are condensed and employed in step (1).
By means of the following Examples, the invention will be explained in more detail. The abbreviations NMOR, NMMO, NMM
and M used in the following to denote N-nitrosomorpholine, N-methylmorpholine-N-oxide, N-methylmorpholine and morpholine respectively.
Example 1 A process liquid from the amine-oxide process, i.e. a residue of a reverse osmosis, was passed over a weak acidic cation exchanger (polyacryl back bone having carboxyl groups as CA 022021~3 1997-04-08 functional groups; Dowex CC-2 made by The Dow Chemical Company). The residue had a pH of 9,9 and the following composition:
NMMO: 1661 ppm NMM: 2377 ppm M: 1376 ppm 30 ml of cation exchanger were used in a column having a diameter of 2,5 cm and a height of approximately 5,5 cm. The residue was passed over the cation exchanger at a flow rate of 4 bed volumes per hour. The eluates were collected in intervals of 5 bed volumes each, and afterwards the pH value and the NMMO, NMM and M concentrations were determined. The cation exchanger started to swell after 10 bed volumes, and the swelling went on continuously until the charging stopped, amounting to 150% after 200 bed volumes.
The NMMO, NMM and M concentrations (ppm) were determined by means of HPLC (column: Hypersil Si 150 x 4 mm; 50C; eluant:
52% of acetonitrile far W, Fisions Scientific Equipment no.
A/0627/17; 48% of 10 mmole KH2PO4 (Merck no. 4873), adjusted to pH 6,7 with NaOH; isocratically lml/min; detector: W 192 nm). The quantification of each of the components was carried out by calibrating an external 3 point gauging. The results are shown in the following Table.
Table Bed NMMO NMM M pH
volume Start 1661 2377 1376 9,9 1 n.d. n.d. 4,0 1 n.d. n.d. 3,9 332 2 n.d. 5,1 2350 1 n.d. 5,8 2409 241 n.d. 7,4 2064 276 2 7,3 2026 1210 3 8,1 1943 1517 5 8,1 1850 2516 6 8,4 1805 2736 6 8,4 100 1671 3461 5 8,5 110 1632 4031 5 8,6 120 1594 4050 6 8,6 130 1594 3919 6 8,6 140 1596 4132 6 8,6 150 1597 4063 7 8,6 160 1596 3939 13 8,6 170 1588 4060 85 8,6 180 1605 3441 459 8,8 190 1625 2723 1422 9,3 200 1620 2390 1875 9,3 210 1646 2390 1748 9,2 n.d. = not detectable As can be seen from the Table, M may be distinctly separated from NMM and NMMO:
In the beginning, each of the three components, i.e. NMMO, NMM and M, is retained by the cation exchanger, and the pH
drops from 9,9 to approximately 4,0.
From the 20th bed volume on, NMMO starts to eluate, while NMM
and M are retained, so that up to the 40th bed volume the eluate actually contains only NMMO. The pH increases to 5,8.
The eluation of NMMO is probably due to a displacement of the NMMO already adsorbed by the cation exchanger by following NMM and M.
From the 40th bed volume on, NMM also starts to eluate, while M is still retained. The pH increases further to approximately 8-9. Obviously the adsorbed NMM is displaced by the following M at the ion exchanger.
CA 02202l~3 l997-04-08 Surprisingly, M is eluated only from approximately the 17Oth bed volume on, i.e. at a point when at least 85 weight% of the NMMO and the NMM have already been recovered. From this point on, the pH increases again to approximately g, 3. Thus the cation exchanger is wholly charged with morpholine and has to be regenerated after 170 bed volumens.
The eluate collected up to the 170th bed volume is actually free from M and may be used for the oxidation treatment to produce NMMO.
Example 2 An aqueous solution cont~in;ng 25 ~g of NMOR, 2530 mg of NMMO, 3923 mg of NMM and 30 mg of M was mixed with 30% H22 (mole NMM/mole H22 = 1/1,2) to oxidize NMM to NMMO and exposed to radiation of a mercury low-pressure lamp in a W
reactor (type EK-36, no. 79000, made by Katadyn) (wavelength:
254 nm). The temperature of the process liquid was 50C.
The NMOR concentration was determined by means of HPLC
(column: Hypersil ODS 250 X 4 mm; 50 C; eluant: A = 0,6% of acetonitrile; B = 49,7% of H2O; gradient 1 ml/min.; 10 min. -100% A; 7 min - 100% B; detector: W 238 nm).
Within the first 90 minutes, the NMOR concentration increased to 45 ~g/l, which is due to a fast reaction of the M present in the solution. Afterwards, the NMOR concentration decreased again rapidly. After 6 hours, there was no evidence of NMOR.
After a total oxidation time of 20 hours, the solution contained 5386 mg of NMMO/litre. This amounts to a yield of 62% of the theory.
The present invention is concerned with a process for the selective separation of morpholine from an aqueous solution cont~;ning morpholine, N-methylmorpholine and N-methylmorpholine-N-oxide. In particular, the present invention is concerned with a process for the regeneration of an aqueous process liquid of the amine-oxide process containing morpholine, N-methylmorpholine and N-methylmorpholine-N-oxide.
For some decades there has been searched for processes for the production of cellulose moulded bodies able to substitute the viscose process, today widely employed. As an alternative which is interesting for its reduced environmental impact among other reasons, it has been found to dissolve cellulose without derivatisation in an organic solvent and extrude from this solution moulded bodies, e.g. fibres, films and other moulded bodies. Fibres thus extruded have received by BISFA
(The International Bureau for the Standardization of man made fibers) the generic name Lyocell. By an organic solvent, BISFA understands a mixture of an organic chemical and water.
It has turned out that as an organic solvent, a mixture of a tertiary amine-oxide and water is particularly appropriate for the production of cellulose moulded bodies. As the amine-oxide, primarily N-methylmorpholine-N-oxide (NMMO) is used.
Other amine-oxides are described e.g. in EP-A - 0 s53 070. A
process for the production of mouldable cellulose solutions is known e.g. from EP-A - 0 356 419. For the purposes of the present specification and the present claims, the production o~ cellulose moulded bodies using tertiary amine-oxides generally is referred to as amine-oxide process.
In EP-A - 0 356 419, an amine-oxide process for the production of spinnable cellulose solutions is described, wherein as a starting material among other substances a suspension of cellulose in liquid, aqueous N-methylmorpholine-N-oxide (NMMO) is used. This process CA 022021~3 1997-04-08 consists in transforming the suspension in a thin-film treatment apparatus in one single step and continuously into a mouldable solution. Finally, the mouldable solution is spun into filaments by a forming tool such as a spinneret and the filaments are passed through a precipitation bath.
In the precipitation bath the cellulose is precipitated. The tertiary amine-oxide is accumulated in the precipitation bath. The precipitation bath may contain up to 30 weight% o~
amine-oxide. For economic reasons of the amine-oxide process it is of vital importance to recover the amine-oxide as completely as possible and reuse it for the production of a mouldable cellulose solution. Thus is is necessary to recover NMMO from the precipitation bath.
A process for the recovery of NMMO from diluted aqueous solutions is known from DD-A - 274 435. According to this process, the aqueous solution is passed over exchanger columns filled with styrene/divinylbenzene copolymer conta;n;ng SO3H groups until it reaches its maximum equimolar exhaustion. Subsequently the NMMO is displaced by equimolar amounts of sodium hydroxide solution and the exchanger columns are regenerated by means of acid.
In addition to the amine-oxide however, the degradation products of the amine-oxide are also accumulated in the precipitation bath. These degradation products may be intensively coloured, thus deteriorating the quality of the cellulose moulded bodies produced. On the other hand, other substances may represent an additional safety risk, since under certain conditions the amine-oxide tends to show highly exothermic decomposition reactions and these decomposition reactions may be induced or accelerated by certain substances. These substances have to be removed from the precipitation bath which is to be regenerated before the NMMO
is concentrated and separated.
CA 022021~3 1997-04-08 After removing these unwanted substances, water is withdrawn from the purified precipitation bath which optionally is combined with other process liquids of the amine-oxide process such as vapour condensates formed during the production of the cellulose solution. This may be carried out for instance by means of evaporation. The residue of this evaporation contains highly concentrated aqueous amine-oxide which is recycled again into the amine-oxide process. The vapours of the evaporation consist mainly of water, wherein considerable amounts of N-methylmorpholine, the main degradation product of NMM0, are also dissolved. Moreover, the vapours contain also NMM0 and morpholine. Typically, the vapours contain up to loo mg of NMMO, 240 mg of N-methylmorpholine and up to 30 mg of morpholine per litre.
Conveniently, these vapours are concentrated, e.g. by means of reverse osmosis. The aqueous solution obtained contains typically up to 4 g of NMMO, up to 10 g of N-methylmorpholine and up to approximately 1 g of morpholine.
From EP-A - 0 402 347 it is known to separate amines from waste waters of cellulose processing by means of a cation exchanger. The cation exchanger carries carboxyl groups as functional groups. Afterwards, the cation exchanger charged with the amines is treated with an aqueous solution of a weak acid having a pKa value of more than 3,0 to eluate the amines. The eluate is regenerated by means of distillation, part of the weak acid being separated from the amines and optionally also recovered. By means of this process, up to 94% of N-methylmorpholine and morpholine in aqueous solutions containing both amines are removed from the waste water. The separated amines are disposed by combustion.
Moreover it is known to separate morpholine, N-methylmorpholine and NMMO together from waste waters by means of a cation exchanger (C. Grilc and N. Zitko, Recovery of Morpholine; Chem. Biochem. Eng. Q. 6 (4), 189-193 (1992)).
CA 022021~3 1997-04-08 EP-A - 0 468 951 describes a process for the separation of amine-oxides from aqueous solutions, particularly waste waters, produced in the cellulose process. According to this known process, the waste waters are contacted with a cation exchanger comprising carboxyl groups as functional groups to charge the cation exchanger with the amine-oxides, whereafter the charged cation exchanger is washed and the amine-oxides are treated with an aqueous solution of a weak acid having a pKa value of more than 3,0 to eluate the amine-oxides. This process also aims at eliminating the amine-oxides completely from the waste waters so as to dispose them in an environmentally friendly way.
In the amine-oxide process however, the NMMO losses should be kept as low as possible. Also, N-methylmorpholine should be oxidized again to NMMO and recovered. Oxidation may be carried out for instance using a peroxidic oxidant.
A process for the preparative production of tertiary amine-oxides by means of oxidation of tertiary amines is known e.g.
from EP-A - 0 092 862. According to this process, the amine-oxide is oxidized under pressure with molecular oxygen in an aqueous solvent, said solvent having a pH value approximately equal or higher than the pKa value of the tertiary amine.
DD-A - 259 863 is concerned with the production of aqueous NMMO solutions by means of oxidation of N-methylmorpholine with H22 and by passing the reaction solution over one or more exchanger columns filled with styrene/divinylbenzene copolymer containing sulphonate groups, as well as by adjusting a pH value of the solution to values ranging from 8 to 5 by addition of phosphoric acid.
In an oxidation it is disadvantageous that morpholine present in the process liquid introduced as a contamination together with the tertiary amines is partially transformed into toxic N-nitrosomorpholine, which is accumulated unwantedly in the CA 022021~3 1997-04-08 NMMO cycle. Additionally, other nitrosoamines are also formed in the oxidation reactions.
Oxidation of N-methylmorpholine with H22 to NMMO is known e.g. from EP-A - 0 254 803. From DE-A - 4 140 259, the production of NMMO by a process wherein the formation of nitrosoamines is restricted by scavenging primary and secondary amines, for instance by means of acid halides, is known. EP-A - 0 320 690 describes the production of-amine-oxides substantially free from nitrosoamines by oxidation with peroxides in the presence of a combination of CO2/ascorbic acid acting as a nitrosoamine inhibitor. From EP-A - 0 401 503, oxidation with H22 in water and a co-solvent, preferably a carboxylic acid ester, is known.
According to FR-A - 8 808 039, oxidation is carried out while adding CO2, and according to US-A - 5,216,154, oxidation to NMMO is carried out in a pure C02 atmosphere.
In the state of the art, the forming of nitrosoamine either is not prohibited, or it is achieved by removing the starting products of the N-nitrosomorpholine or by employing additives to slow down the formation rate of the N-nitrosomorpholine.
Particularly in an amine-oxide process comprising a closed cycle, the addition of various chemicals such as acid halides or ascorbic acid or CO2 to the process causes problems in the purification of the process liquids, since the degradation products introduced together with the added chemicals have to be removed from the process. For many chemicals, it is also necessary to consider safety aspects such as the risk of exothermic reactions. Thus, neither of the described processes is appropriate for the regeneration of process liquids of the amine-oxide process.
Thus it is the object of the present invention to provide a process for the selective separation of morpholine from various process liquids of the amine-oxide process wherein substantially only morpholine is separated and NMMO and N-methylmorpholine will remain in the process liquid.
CA 022021~3 1997-04-08 The process according to the invention for selective separation of morpholine from an aqueous solution cont~in;ng morpholine, N-methylmorpholine and NMMO is characterized by the following steps:
(A) passing the aqueous solution over a cation exchanger capable of adsorbing morpholine in such an amount until it cannot be charged substantially with morpholine any more and an eluate substantially free from morpholine but cont~in;ng N-methylmorpholine and N-methylmorpholine-N-oxide is obtained, and (B) regenerating the cation exchanger charged with morpholine and reusing it in step (A).
The present invention is based upon the finding that a cation exchanger evidently has a higher activity for morpholine than for N-methylmorpholine and NMMO and that due to this higher activity a high yield of N-methylmorpholine and NMMO has already been eluated the moment morpholine starts to break through, thus allowing a distinct separation of the morpholine. In detail, the separation is carried out such that first each of the three components, i.e. morpholine, N-methylmorpholine and NMMO, are adsorbed at the fresh cation exchanger. When the cation exchanger is charged with these three components, NMMO starts to break through, since on the one hand the following NMMO cannot be adsorbed any more and on the other the following morpholine and N-methylmorpholine displace the NMMO already adsorbed. This means that the eluate contains at that point actually only NMMO.
When substantially all the NMMO is displaced at the cation exchanger, N-methylmorpholine also appears in the eluate, being displaced by the following morpholine. At that point, the eluate contains NMMO and N-methylmorpholine. Only when substantially no N-methylmorpholine is adsorbed at the cation exchanger and the capacity of the cation exchanger is exhausted, morpholine starts to break through and the CA 022021~3 1997-04-08 eluation has to be interrupted and the cation exchanger regenerated. This can be done for instance using diluted mineral acids.
The cation exchanger employed in the process according to the invention exhibits preferably carboxyl groups and/or sulphonic acid groups.
A preferred embodiment of the process according to the invention is characterized by the further step of (C) subjecting the eluate obtained in step (A) to an oxidation treatment optionally after water has been removed to oxidize N-methylmorpholine to N-methylmorpholine-N-oxide.
This embodiment of the process according to the invention completely prevents the new formation of the toxic N-nitrosomorpholine, since the eluate contains actually no morpholine. Thus the oxidized eluate contains only the usual reduced basic level of N-nitrosomorpholine which occurs in the amine-oxide process.
Conveniently, oxidation is carried out by means of a peroxidic oxidant. As the peroxidic oxidant, in the process according to the invention preferably H22 is used. The H22 is employed preferably as an aqueous solution having 30-50 weight% of H202. The H22 is best employed in an amount of from 0,8 to 2 mole per mole of N-methylmorpholine.
Another preferred embodiment of the process according to the invention is characterized in that the aqueous solution is exposed to ultraviolet radiation having substantially a wavelength of 254 nm during or subsequently to the oxidation treatment. The ultraviolet radiation is best emitted by a mercury low-pressure lamp.
CA 022021~3 1997-04-08 This embodiment of the process according to the invention is based on the finding that N-nitrosomorpholine can be destroyed by exposure to ultraviolet radiation having an intensity maximum of 254 nm. Therefore, when exposure to ultraviolet radiation is carried out during or subsequently to the oxidation treatment, destruction of the N-nitrosomorpholine present at a basic level will occur, and thus it becomes possible to significantly reduce the basic level of this toxic substance.
It has been shown that it is more advantageous to first separate morpholine by means of the cation exchanger and then proceed to oxidize the eluate, since thus the exposure time to ultraviolet radiation and the exposure intensity necessary to destroy the N-nitrosomorpholine are significantly reduced.
When morpholine is not separated before oxidation, an amount of N-nitrosomorpholine equivalent to the morpholine content will be formed again, requiring a significantly higher exposure time and rate for destruction.
The exposure rate may range e.g. from 200 to 500 mJ/cm2, depending on the design of the lamp and the process conditions, particularly the temperature.
General methods for the quantitative analysis of nitrosoamines which use a W exposure and a subsequent determination of the nitrites formed are known (D.E.G.
Shuker, S.R. Tannenbaum, Anal. Chem., 1983, 55, 2152-2155; M.
Rhighezza, M.H. Murello, A.M. Siouffi, J. Chromat., 1987, 410, 145-155; J.J. Conboy, J.H. Hotchkiss, Analyst, 1989, 114, 155-159; B. Buchele, L. Hoffmann, J. Lang, Fresen.J.Anal.Chem., 1990, 336, 328-333). These analytic methods however do not deal with the destruction of N-nitrosomorpholine.
For exposure according to the invention using a low-pressure lamp, the lamp may be hung into a container containing the process liquid which is to be treated. However the lamp may also be arranged in another way. Moreover, exposure may be carried out for instance during a continuous pumping over of the solution to be exposed in a thin-film W-reactor.
The process according to the invention is particularly appropriate for regeneration of a process liquid from the amine-oxide process.
Another preferred embodiment of the process according to the invention comprises the following steps:
(1) passing the above vapours concentrated for instance by means of reverse osmosis over a cation exchanger capable of selectively adsorbing morpholine and safeguarding that the pH value lies in a range of from 6,0 to 9,0, thereafter (2) combining the eluate obtained from the cation exchanger with purified precipitation bath of the amine-oxide process, said precipitation bath containing 10-30 weight%
of NMMO and (3) treating the eluate combined with the precipitation bath in an evaporation reactor with the peroxidic oxidant to oxidize N-methylmorpholine and to concentrate, obtaining concentrated, aqueous NMMO which is recycled again into the amine-oxide process and vapours which are condensed and employed in step (1).
By means of the following Examples, the invention will be explained in more detail. The abbreviations NMOR, NMMO, NMM
and M used in the following to denote N-nitrosomorpholine, N-methylmorpholine-N-oxide, N-methylmorpholine and morpholine respectively.
Example 1 A process liquid from the amine-oxide process, i.e. a residue of a reverse osmosis, was passed over a weak acidic cation exchanger (polyacryl back bone having carboxyl groups as CA 022021~3 1997-04-08 functional groups; Dowex CC-2 made by The Dow Chemical Company). The residue had a pH of 9,9 and the following composition:
NMMO: 1661 ppm NMM: 2377 ppm M: 1376 ppm 30 ml of cation exchanger were used in a column having a diameter of 2,5 cm and a height of approximately 5,5 cm. The residue was passed over the cation exchanger at a flow rate of 4 bed volumes per hour. The eluates were collected in intervals of 5 bed volumes each, and afterwards the pH value and the NMMO, NMM and M concentrations were determined. The cation exchanger started to swell after 10 bed volumes, and the swelling went on continuously until the charging stopped, amounting to 150% after 200 bed volumes.
The NMMO, NMM and M concentrations (ppm) were determined by means of HPLC (column: Hypersil Si 150 x 4 mm; 50C; eluant:
52% of acetonitrile far W, Fisions Scientific Equipment no.
A/0627/17; 48% of 10 mmole KH2PO4 (Merck no. 4873), adjusted to pH 6,7 with NaOH; isocratically lml/min; detector: W 192 nm). The quantification of each of the components was carried out by calibrating an external 3 point gauging. The results are shown in the following Table.
Table Bed NMMO NMM M pH
volume Start 1661 2377 1376 9,9 1 n.d. n.d. 4,0 1 n.d. n.d. 3,9 332 2 n.d. 5,1 2350 1 n.d. 5,8 2409 241 n.d. 7,4 2064 276 2 7,3 2026 1210 3 8,1 1943 1517 5 8,1 1850 2516 6 8,4 1805 2736 6 8,4 100 1671 3461 5 8,5 110 1632 4031 5 8,6 120 1594 4050 6 8,6 130 1594 3919 6 8,6 140 1596 4132 6 8,6 150 1597 4063 7 8,6 160 1596 3939 13 8,6 170 1588 4060 85 8,6 180 1605 3441 459 8,8 190 1625 2723 1422 9,3 200 1620 2390 1875 9,3 210 1646 2390 1748 9,2 n.d. = not detectable As can be seen from the Table, M may be distinctly separated from NMM and NMMO:
In the beginning, each of the three components, i.e. NMMO, NMM and M, is retained by the cation exchanger, and the pH
drops from 9,9 to approximately 4,0.
From the 20th bed volume on, NMMO starts to eluate, while NMM
and M are retained, so that up to the 40th bed volume the eluate actually contains only NMMO. The pH increases to 5,8.
The eluation of NMMO is probably due to a displacement of the NMMO already adsorbed by the cation exchanger by following NMM and M.
From the 40th bed volume on, NMM also starts to eluate, while M is still retained. The pH increases further to approximately 8-9. Obviously the adsorbed NMM is displaced by the following M at the ion exchanger.
CA 02202l~3 l997-04-08 Surprisingly, M is eluated only from approximately the 17Oth bed volume on, i.e. at a point when at least 85 weight% of the NMMO and the NMM have already been recovered. From this point on, the pH increases again to approximately g, 3. Thus the cation exchanger is wholly charged with morpholine and has to be regenerated after 170 bed volumens.
The eluate collected up to the 170th bed volume is actually free from M and may be used for the oxidation treatment to produce NMMO.
Example 2 An aqueous solution cont~in;ng 25 ~g of NMOR, 2530 mg of NMMO, 3923 mg of NMM and 30 mg of M was mixed with 30% H22 (mole NMM/mole H22 = 1/1,2) to oxidize NMM to NMMO and exposed to radiation of a mercury low-pressure lamp in a W
reactor (type EK-36, no. 79000, made by Katadyn) (wavelength:
254 nm). The temperature of the process liquid was 50C.
The NMOR concentration was determined by means of HPLC
(column: Hypersil ODS 250 X 4 mm; 50 C; eluant: A = 0,6% of acetonitrile; B = 49,7% of H2O; gradient 1 ml/min.; 10 min. -100% A; 7 min - 100% B; detector: W 238 nm).
Within the first 90 minutes, the NMOR concentration increased to 45 ~g/l, which is due to a fast reaction of the M present in the solution. Afterwards, the NMOR concentration decreased again rapidly. After 6 hours, there was no evidence of NMOR.
After a total oxidation time of 20 hours, the solution contained 5386 mg of NMMO/litre. This amounts to a yield of 62% of the theory.
Claims (8)
1. A process for the selective separation of morpholine from an aqueous solution containing morpholine, N-methylmorpholine and N-methylmorpholine-N-oxide, characterized by the following steps:
(A) passing said aqueous solution over a cation exchanger capable of adsorbing morpholine in such an amount until it cannot be charged substantially with morpholine any more and an eluate substantially free from morpholine but containing N-methylmorpholine and N-methylmorpholine-N-oxide is obtained, and (B) regenerating said cation exchanger charged with morpholine and reusing it in step (A).
(A) passing said aqueous solution over a cation exchanger capable of adsorbing morpholine in such an amount until it cannot be charged substantially with morpholine any more and an eluate substantially free from morpholine but containing N-methylmorpholine and N-methylmorpholine-N-oxide is obtained, and (B) regenerating said cation exchanger charged with morpholine and reusing it in step (A).
2. A process according to Claim 1, characterized in that said cation exchanger comprises carboxyl groups.
3. A process according to Claim 1, characterized in that said cation exchanger comprises sulphonic acid groups.
4. A process according to one of the Claims 1 to 3, characterized by the further step of (C) subjecting the eluate obtained in step (A) to an oxidation treatment optionally after water has been removed to oxidize N-methylmorpholine to N-methylmorpholine-N-oxide.
5. A process according to Claim 4, characterized in that oxidation is carried out by means of a peroxidic oxidant.
6. A process according to one of the Claims 4 or 5, characterized in that said aqueous solution is exposed to ultraviolet radiation having substantially a wavelength of 254 nm during or subsequently to said oxidation treatment.
7. A process according to Claim 6, characterized in that said ultraviolet radiation is emitted by a mercury low-pressure lamp.
8. A process according to one of the Claims 1 to 7, characterized in that as said aqueous solution containing morpholine, N-methylmorpholine and N-methylmorpholine-N-oxide a process liquid from the amine-oxide process is employed.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT140395A AT403297B (en) | 1995-08-18 | 1995-08-18 | METHOD FOR SELECTIVE SEPARATION OF MORPHOLINE |
| ATA1403/95 | 1995-08-18 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2202153A1 true CA2202153A1 (en) | 1997-02-27 |
Family
ID=3513141
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2202153 Abandoned CA2202153A1 (en) | 1995-08-18 | 1996-08-16 | Process for the selective separation of morpholine |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0783497A1 (en) |
| JP (1) | JPH10508318A (en) |
| CN (1) | CN1071750C (en) |
| AT (1) | AT403297B (en) |
| AU (1) | AU700207B2 (en) |
| BR (1) | BR9606585A (en) |
| CA (1) | CA2202153A1 (en) |
| NO (1) | NO310572B1 (en) |
| WO (1) | WO1997007108A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19842556C2 (en) * | 1998-09-17 | 2003-02-06 | Alceru Schwarza Gmbh | Process for the production of cellulosic moldings |
| US20210016204A1 (en) * | 2018-03-15 | 2021-01-21 | Basf Se | Process for removing methoxyethanol from a mixture comprising methoxyethanol and morpholine |
| CN110563669A (en) * | 2019-10-09 | 2019-12-13 | 四川鸿鹏新材料有限公司 | Method and device for improving morpholine purity |
| CN112480035A (en) * | 2020-10-28 | 2021-03-12 | 华茂伟业绿色科技股份有限公司 | N-methylmorpholine and purification method thereof, methylmorpholine oxide and preparation method thereof |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DD254199B5 (en) * | 1986-12-04 | 1994-01-05 | Thueringische Faser Ag Schwarz | PROCESS FOR CLEANING WAFERRIGER N-METHYLMORPHOLIN N-OXYD SOLUTIONS |
| DD259863A1 (en) * | 1987-04-06 | 1988-09-07 | Schwarza Chemiefaser | METHOD FOR PRODUCING WAFERRIGER, PURE N-METHYLMORPHOLIN N-OXIDE SOLUTIONS |
| DD274435B5 (en) * | 1988-08-02 | 1996-10-31 | Thueringisches Inst Textil | Process for the recovery of N-methylmorpholine-N-oxide |
| AT393114B (en) * | 1989-06-08 | 1991-08-26 | Chemiefaser Lenzing Ag | METHOD FOR SEPARATING AMINES |
| AT392915B (en) * | 1990-03-28 | 1991-07-10 | Chemiefaser Lenzing Ag | METHOD FOR SEPARATING WATER FROM A DILUTED AQUEOUS SOLUTION OF N-METHYLMORPHOLIN-N-OXIDE, N-METHYLMORPHOLIN AND / OR MORPHOLIN |
-
1995
- 1995-08-18 AT AT140395A patent/AT403297B/en not_active IP Right Cessation
-
1996
- 1996-08-16 WO PCT/AT1996/000146 patent/WO1997007108A1/en not_active Application Discontinuation
- 1996-08-16 EP EP96926960A patent/EP0783497A1/en not_active Ceased
- 1996-08-16 AU AU66954/96A patent/AU700207B2/en not_active Ceased
- 1996-08-16 BR BR9606585A patent/BR9606585A/en not_active Application Discontinuation
- 1996-08-16 CN CN96191128A patent/CN1071750C/en not_active Expired - Fee Related
- 1996-08-16 JP JP9508733A patent/JPH10508318A/en not_active Ceased
- 1996-08-16 CA CA 2202153 patent/CA2202153A1/en not_active Abandoned
-
1997
- 1997-04-17 NO NO19971753A patent/NO310572B1/en not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| CN1071750C (en) | 2001-09-26 |
| CN1165514A (en) | 1997-11-19 |
| EP0783497A1 (en) | 1997-07-16 |
| ATA140395A (en) | 1997-05-15 |
| WO1997007108A1 (en) | 1997-02-27 |
| BR9606585A (en) | 1997-10-28 |
| NO310572B1 (en) | 2001-07-23 |
| AU6695496A (en) | 1997-03-12 |
| JPH10508318A (en) | 1998-08-18 |
| NO971753L (en) | 1997-04-17 |
| AU700207B2 (en) | 1998-12-24 |
| AT403297B (en) | 1997-12-29 |
| NO971753D0 (en) | 1997-04-17 |
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