PROCESS FOR THE PRODUCTION OF DICHLOROHYDRIN

Abstract: The invention relates to a continuous process for the produc­ tion of an organic solvent solution of dichlorohydrin, which comprises: a) reacting allyl chloride, water and chlorine in a reaction zone to form an aqueous solution of dichlorohydrin, b) contacting in an extraction zone the reaction zone effluent with a water-immiscible inert organic solvent for the dichloro­ hydrin to obtain a dichlorohydrin-enriched solvent and an aqueous phase, c) passing said dichlorohydrin-enriched solvent from said extrac­ tion zone, d) passing said aqueous phase from the extraction zone to an electrodialysis zone, e) electrodialyzing said aqueous phase in said electrodialysis zone to obtain: (1) a concentrate stream having chloride content higher than said aqueous phase, and (2) a diluate stream having chloride content lower than said aqueous phase, f) withdrawing said concentrate stream, and g) recycling at least part of said diluate stream from step (e) to the reaction zone of step (a).

Description: It is known to prepare dichlorohydrin by reacting in a reaction zone allyl chloride, water and chlorine in dilute aqueous phase, see U.S. Patent Specifications 2,714,121 and 2,714,123. The term "dichlorohydrin" herein designates the isomers 2,3-dichloro-1-­ propanol and 1,3-dichloro-2-propanol. The reaction zone effluent may be worked up in various ways to recover the dichlorohydrin therefrom, or may be processed further in an integrated process to convert the chlorohydrins to derivatives such as epichlorohydrin and/or glycerine. It is known from Belgian Patent Specifications 614,890 and 614,891 that dichlorohydrin may be extracted from aqueous solution with organic solvents such as phosphate esters of aliphatic mono­ hydric alcohols containing more than four carbon atoms, aryl phosphates, and liquid aliphatic alcohols and liquid ketones having 8 to 18 carbon atoms per molecule. U.S. Patent Specification 3,909,382 discloses recovering acid values such as hydrochloric acid formed during olefin chlorohydrina­ tion by series flow through a plurality of electrodialysis stages to upgrade the acid to higher concentration. One disadvantage of the known processes is that substantial amounts of water are used in the reaction zone of the process to reduce formation of undesired by-products, which by-products reduce the overall efficiency of the process and may complicate purifica­ tion procedures of the desired product. Such conventional processes result in an aqueous effluent stream which contains minor amounts of organic impurities diluted in a substantial amount of water. Such effluent requires energy intensive treatment to reduce the amount of organic materials to levels acceptable to be passed to receiving bodies of water such as rivers, lakes and the like. Considerable savings could be effected if the amount of water to be treated could be significantly reduced. According to the invention, there is provided in a continuous process for the production of an organic solvent solution of dichlorohydrin comprises: a) reacting allyl chloride, water and chlorine in a reaction zone to form an aqueous solution of dichlorohydrin, b) extracting in an extraction zone the reaction zone effluent with a water-immiscible inert organic solvent for the dichloro­ hydrin to obtain a dichlorohydrin-enriched solvent and an aqueous phase, c) passing said dichlorohydrin-enriched solvent from said extrac­ tion zone, d) passing said aqueous phase from the extraction zone to an electrodialysis zone, e) electrodialyzing said aqueous phase in said electrodialysis zone to obtain: (1) a concentrate stream having chloride content higher than said aqueous phase, and (2) a diluate stream having chloride content lower than said aqueous phase, f) withdrawing said concentrate stream, and g) recycling at least part of said diluate stream from step (e) to the reaction zone of step (a). By this continuous process the quantity of fresh water used is reduced. In the principal reaction, allyl chloride is converted to a mixture of the two isomers of glycerol dichlorohydrin by reaction with hypochlorous acid, HCIO, which is readily formed when chlorine is dissolved in water. The chlorohydrination reaction takes place readily at temperatures in the range from 15 to 55 °C. Decreased temperature rapidly increases the amount of dissolved chlorine as well as the concentration of the hypochlorous acid. For maximum dichlorohydrin yield it is necessary to run the reaction at low concentrations of chloride ion and of chlorohydrin, i.e., with high water dilution. The presence of excess allyl chloride during the reaction typically results in the formation of undesired by-­ products. Inert organic solvents suitably employed to effectively remove glycerol dichlorohydrins from aqueous solution include liquid organic esters, especially phosphate esters, which are immiscible with water. Preferred are esters containing from 4 to 28 carbon atoms, especially from 6 to 18 carbon atoms. Representative com­ pounds are n-butyl acetate, tributylphosphate, tri-(2-ethylhexyl)-­ phosphate, butyl dioctylphosphate, tri-n-octylphosphate, trihexyl­ phosphate, tridecylphosphate and trioctadecylphosphate. Exemplary aryl phosphates include tricresyl phosphate, dicresyl phosphate, diphenyl cresyl phosphate, triphenyl phosphate, 2-ethylhexyl-­ diphenyl phosphate, o-chlorophenyldiphenyl phosphate, bis-(p-tert­ butylphenyl) phenyl phosphate and didecylphenyl phosphate. The phosphate esters, if desired, may be combined with one or more of various liquid hydrocarbon thinners to result in a more desirable density or viscosity of the solvent phase. The thinner should, of course, be inert to the reaction components and insoluble in the aqueous phase. Exemplary which may be used as solvents or as thinners include hexane, benzene, heptane, n-octane, methylcyclo­ hexane, petroleum naphthas and kerosene. Additional solvents include liquid aliphatic alcohols and ketones containing from 4 to 18 carbon atoms especially from 5 to 18 carbon atoms. Representative compounds include methyl isobutyl ketone, n-hexanol isodecanol, isobutyl heptyl ketone, 5-ethyl-2-no­ nanol, 7-ethyl-2-methyl-4-undecanol, heptadecanol, oleyl alcohol, linolyl alcohol, 1-nonanol, 2-nonanol, diisobutylcarbinol, diiso­ butyl ketone, 2-nonanone, 5-nonanone, lauryl alcohol, 1-hendecanol, 3-hendecanone, diisomayl ketone and 4-decanone. Although chloro- ­ and nitro-substituted derivatives of said compounds may also be suitable, preferred among those compounds as solvent is a saturated aliphatic alcohol or ketone. Further solvents include ethers such as ethyl ether and isopropyl ether and chlorinated hydrocarbons such as methylene chloride, chloroform, carbon tetrachloride and trichloropropane. Preferred among those compounds as solvent is a saturated aliphatic ether or chlorinated hydrocarbon containing up to 9, preferably up to 8 carbon atoms. The extraction is carried out employing conventional extraction techniques, wherein the dichlorohydrin is extracted into the solvent. The solvent is then removed from the remaining aqueous phase, following which the solvent may be distilled off from the dichlorohydrin and recycled to the extraction zone. The reaction zone effluent typically has a low pH e.g. 0.3 to 1.0, resulting from the formation of hydrogen chloride as by-product in the formation of the dichlorohydrin. It is preferred that the effluent prior to extraction be partially neutralized to a pH in the range from 1.5 to 7.0 and preferably from 5.0 to 6.5 by the addition of a basic compound such as an alkali metal hydroxide. This may facilitate both the separation of the solutions in the extraction step and subsequent electrodialysis of the aqueous raffinate. An additional advantage is that the less corrosive nature of the effluent will permit a wider choice of less expensive materials of construction in the extraction zone. After the extraction the aqueous phase is passed to an electrodialysis step. Electrodialysis is by now a well established industrial process. Basically, an electrodialysis unit comprises a plurality of membranes alternately anionic and cationic placed between an anode and a cathode connected to a direct current source. The membranes are usually separated from each other by 1 to 5 mm using appropriate spacers and the feed stream may be made to flow through a spacer creating a turbulent path in order to increase turbulence of the liquids contacting the membranes, or insheet-type flow to reduce pumping pressure. The construction of the unit is generally in the form of a stack, like a filter stack. The membranes which usually contain ion exchange groups have a fixed positive or negative charge. The cationic membranes have negative fixed charges; the anionic membranes have positive fixed charges. Electrical neutrality in the membrane matrix is satisfied by the migrating cations (through cationic membranes) and anions, (through anionic exchange membranes). When a direct current is applied across the two electrodes (anode and cathode), anions will tend to migrate towards the anode passing through the anion exchange membrane and being stopped by the first cation exchange membrane. In like manner, cations will cross through the cationic exchange membrane and will be stopped by the anionic exchange membranes. However, non-electrolyte species are not prevented from passing through the exchange membranes, except in so far as these are made of a tighter pore structure. Even so, non-electrolytes may migrate through the membranes, the actual amount of migration depending on relative volume of diluate/concentrate. If a feed stream is introduced uniformly to electrodialysis unit, it will be found that passages in the unit having an anion membrane on the cathode side of the passage and vice versa will become concentrate streams richer in ionized (herein saline) components and the other streams in passages bounded by anion membranes on the anode side and cathode membranes on the cathode side will become depleted in ionized components. Such depleted stream or streams are herein referred to as the diluate stream. The anionic and cationic membranes employed herein are known in the art. Generally, the anionic and cationic membranes comprise flat sheets of inorganic or organic materials which have extreme water-insolubility. Preferably the anionic and cationic membranes are prepared from synthetic organic resinous, polymeric materials, (e.g., polystyrene polymers) to which are bonded ionic groups. Any strong or weak base (e.g., tertiary amines or quaternary ammonium compounds) can be chemically bonded to the organic material to form cationic membranes; any strong or weak acid (e.g., aryl sulphonates) can be chemically bonded to the organic resinous material to form anionic membranes. Generally, the anionic and cationic membranes herein, either in the form of a homogeneous sheet or cast, are backed or reinforced with an embedded screen or matrix of synthetic reinforcing fabric, for example, fibreglass or dynel (modified acrylic polymer) to provide them with a substantially rigid structure. Other backings can be used, provided the anionic and cationic membranes remain essentially impervious to mass flow but porous enough to permit ion migration or transfer. The cation and anion-exchange membranes can be any cation- and anion-selective membranes respectively which are essentially stable in the feed water and not chemically degraded by the components therein. Exemplary membranes are disclosed in the article entitled "Electrodiolysis", Kirk-Othmer, Encyclopedia of Science and Technology, pages 846-865 (Second Edition, Interscience Publishers, 1965) and U.S. Patent Specifications Nos. 2,730,768, 2,762,272, 2,860,097 and 3,616,385. Generally, for stability of the membranes, it is necessary to employ temperatures below 70 °C during electrodialysis. While in terms of electrical efficiency it would be preferred to carry out the electrodialysis step at about 50 °C, experience thus far has shown best results are obtained at a temperature in the range from 35 to 45 °C. The diluate stream after the electrodialysis step is substantially depleted in undesirable ions and is recycled to the reaction zone, thereby reducing by a like amount the quantity of fresh i.e., unused water required for high yield production of the dichlorohydrin. The concentrate stream 64 from the electrodialysis step has considerably reduced volume to be handled for subsequent treatment or disposal. An embodiment of the invention will now be described with reference to the accompanying drawing which shows diagrammatically a preferred assemblage adapted to the continuous manufacture of dichlorohydrin. Although the reaction stages in this embodiment are shown to be circulating loop reactors, as will be obvious to those skilled in the art the reaction stages suitably can be stirred reactors such as e.g., vane disc turbine dispersers, sprayed towers or other equipment known to be suitable for chlorohydrin reactions. Referring to the drawing, a fresh water stream is continuously introduced through conduit 10 into a first stage reaction loop comprising conduits 12, 14, 16, pump 18, conduits 20, 22, motor driven mixer 24 and conduits 26 and 28. Allyl chloride is continuously fed into the water stream through conduit 15, while chlorine in an amount substantially equimolar with respect to the allyl chloride is fed to the reaction loop through conduit 21. The relatively dilute reaction mixture is circulated through the loop and a portion of the mixture after passing through pump 18 and mixer 24 is continuously diverted via conduit 30 to the second stage, a like reaction loop comprising conduits 32 and 34, pump 36, conduits 38 and 40, mixer 42, and conduits 44 and 46. The diverted portion of the first stage reaction effluent forms the make-up liquid added to the reaction mixture in the stage where further quantities of allyl chloride and chlorine are added via conduits 33 and 39 respectively. A portion of the stream in line 44, which is more concentrated than that in line 26 is continuously discharged as product. Additional reaction stages, for example three, four, five or more, could be employed, as desired, serving to further decrease the formation of by-products in the aqueous phase. It is preferred that substantially all of the water be added to the first in the series of reaction stages since this represents the most efficient method of operation. The final concentration of the aqueous reaction mixture may vary within relatively wide limits. Preferably the total of from 0.02 to 0.1 volume of allyl chloride (and a substantially equimolar quantity of chlorine) is added for each volume of water supplied to the system. The reaction may be conducted within a wide temperature range and under atmospheric, subatmospheric or superatmospheric pressures. In general, reaction temperatures between 15 and 75 °C, preferably between 25 and 55 °C can be employed. The reaction between allyl chloride and hypochlorous acid (formed in-situ by the reaction of chlorine and water) proceeds rapidly and is normally complete within one or two seconds, however, total residence times in the reaction zone (total of all stages) of from 1 to 10 minutes may be employed. The total residence time is determined by dividing the total volume of the system by the rate of reaction product draw off per minute. A basic material is added to the reaction zone effluent via conduit 50 to partially neutralize the effluent to a pH in the range from 5 to 6.5. Although in theory any basic material may be added, it is found that poorly soluble materials such as lime and calcium carbonate tend to promote the formation of emulsions in the subsequent extraction step (A). Accordingly, it is preferred that the basic material be a solution of soluble hydroxide or carbonate of a Group I metal such as lithium, potassium or sodium. Of these, sodium hydroxide is preferred owing to its lower cost and ready availability. The reaction zone effluent after adjustment of the pH is passed via conduit 52 to extraction zone 54 which may be any conventional liquid-liquid extractor such as an agitated vessel, jet mixer, or perforated plate tower, but preferably is a rotating disc contactor, as shown. Although cocurrent extraction may be suitable, counter-current extraction is preferred. As illustrated in the drawing, the reaction zone effluent enters near the top of extraction zone 54 and the down-flowing aqueous phase contacts upflowing inert organic solvent which is less dense than water such as isopropyl ether entering the lower part of the extraction zone via conduit 56. As will be understood by those skilled in the art, when employing an inert organic solvent having a density greater than the reaction mixture e.g., carbon tetrachloride, the more dense solvent would be introduced near the top of the extraction zone, and the reaction effluent would enter near the bottom of the extraction zone. The rotating centre shaft of the contactor shown is equipped with disc baffles to facilitate extraction of the dichlorohydrin from the downflowing reaction zone aqueous phase into the upflowing inert organic solvent. Generally, substantially complete extraction of the dichlorohydrin present can be achieved if the solvent is contacted with the aqueous phase in a solvent to aqueous phase weight ratio of from 1:1 to 1:20, with weight ratio of 1:2 to 1:10 being preferred. The dichlorohydrin-fat solvent then passes from the extraction zone 54 via conduit 58 for separation of the solvent from the dichlorohydrin (not shown) and is recycled (not shown) to the extraction zone via conduit 56, with or without intermediate storage, as desired. As will be apparent to those skilled in the art, the temperature of the extraction step can be suitably controlled by adjusting the temperature of the solvent added. Further, in order to compensate for minor solvent losses through the process, a small amount of solvent may be added along with the recycle solvent (not shown) to maintain the desired ratio of solvent to reaction zone effluent in the extracting step of the process. The dichlorohydrin-depleted aqueous phase is removed from the bottom of extraction zone 54 via conduit 60 and is passed to electrodialysis zone 62. If desired the aqueous phase from the extraction zone may be passed via an intermediate stripping zone (not shown) to substantially remove any entrained organic solvent. The aqueous phase exiting the extraction zone at a rate of e.g., 3785 litres per minute and having a concentration of about 0.4N sodium chloride along with 0.5 to 1 per cent by weight organic components is then fed to an electrodialysis unit 62 comprised of alternating anionic exchange membranes 103 QZL 386 and cation exchange membranes 61 AZL 386 which membranes are available from Ionics, Inc. About 96 per cent of the sodium chloride in the feed is removed. In general, the voltage across each stack of membranes is arranged so that there is a voltage of 0.5 to 3.0 volts per cell pair, with a voltage of 0.8 to 2 volts being preferred. The concentrate stream from the electrodialysis unit having a volume of about 378 litres per min and containing about 0.4N NaCl is removed via conduit 64, and may be disposed as such or subjected to further treatment, as desired. The diluate comprising about 3400 litres per min flow and containing only about 1000 ppmw of sodium chloride is recycled via conduit 66 to the first stage of the reaction zone, thereby substantially reducing the amount of fresh water required to be fed to the process.

Claims: 1. A continuous process for the production of an organic solvent solution of dichlorohydrin, which comprises: a) reacting allyl chloride, water and chlorine in a reaction zone to form an aqueous solution of dichlorohydrin, b) contacting in an extraction zone the reaction zone effluent with a water-immiscible inert organic solvent for the dichloro­ hydrin to obtain a dichlorohydrin-enriched solvent and an aqueous phase, c) passing said dichlorohydrin-enriched solvent from said extrac­ tion zone, d) passing said aqueous phase from the extraction zone to an electrodialysis zone, e) electrodialyzing said aqueous phase in said electrodialysis zone to obtain: (1) a concentrate stream having chloride content higher than said aqueous phase, and (2) a diluate stream having chloride content lower than said aqueous phase, f) withdrawing said concentrate stream, and g) recycling at least part of said diluate stream from step (e) to the reaction zone of step (a). 2. A process as claimed in claim 1 wherein the organic solvent is an ester, aliphatic alcohol or aliphatic ketone containing from 4 to 18 carbon atoms. 3. A process as claimed in claim 1 wherein the organic solvent is a saturated aliphatic ether or a dichlorinated hydrocarbon containing up to 9 carbon atoms. 4. A process as claimed in claims 1-3, wherein in step (d) the aqueous phase contains from 0.1 to 0.6N of sodium chloride. 5. A process as claimed in claim 1 wherein in step (g) the amount of diluate recycled to the reaction zone is from 10 to 90 %v of the water fed to the reaction zone. 6. A process as claimed in claims 1-5, wherein the temperature of the reaction zone is controlled by controlling the temperature of the inert organic solvent entering the extraction zone. 7. A process as claimed in claim 1, wherein intermediate to steps a) and b), the reaction mixture is partially neutralized to a pH in the range from 0.5 to 6.5.

Inventors: BLYTAS, GEORGE CONSTANTIN, FOSTER, ELTON GORDON, GRIMSBY, FRANK NORMAN
Applicants: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Application year: 1986
Main classification: C07C29
IPC codes: C07C29, C25B7, B01D57, C07C31, B01D61, C07C27, C07C67