WO2001046109A1 - Procede d"elimination amelioree d"acetone issue de processus de carbonylation - Google Patents

Procede d"elimination amelioree d"acetone issue de processus de carbonylation Download PDF

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Publication number
WO2001046109A1
WO2001046109A1 PCT/US2000/030989 US0030989W WO0146109A1 WO 2001046109 A1 WO2001046109 A1 WO 2001046109A1 US 0030989 W US0030989 W US 0030989W WO 0146109 A1 WO0146109 A1 WO 0146109A1
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Prior art keywords
acetone
stream
methyl acetate
methyl iodide
distillation zone
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PCT/US2000/030989
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English (en)
Inventor
Joseph Nathaniel Bays
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Eastman Chemical Company
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Publication date
Application filed by Eastman Chemical Company filed Critical Eastman Chemical Company
Priority to JP2001546623A priority Critical patent/JP2003518053A/ja
Priority to BR0016571-9A priority patent/BR0016571A/pt
Priority to EP00977156A priority patent/EP1240128A1/fr
Publication of WO2001046109A1 publication Critical patent/WO2001046109A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/10—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide
    • C07C51/12—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide on an oxygen-containing group in organic compounds, e.g. alcohols
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/38—Separation; Purification; Stabilisation; Use of additives
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/78—Separation; Purification; Stabilisation; Use of additives
    • C07C45/80—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/78—Separation; Purification; Stabilisation; Use of additives
    • C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
    • C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/78—Separation; Purification; Stabilisation; Use of additives
    • C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
    • C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
    • C07C45/83—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation by extractive distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
    • C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation

Definitions

  • the present invention relates to an improved process of removal of acetone formed during the production of acetic anhydride by carbonylation. More particularly, the present invention relates to a separation process for removing acetone from a mixture which includes an alkyl halide, methyl acetate and acetone.
  • carbonylation processes in particular rhodium catalyzed carbonylation processes, have become industrially important.
  • One such important carbonylation process is for the production of acetic anhydride and the coproduction of acetic acid by contacting a mixture which includes methyl iodide and methyl acetate and/or dimethyl ether with carbon monoxide in the presence of a rhodium catalyst.
  • Such rhodium catalysis processes are well known in the art and have been the subject of numerous patents.
  • acetone An unwanted byproduct, acetone, is formed in the above-described carbonylation process, and typically accumulates in the acetic anhydride production system to a maximum level of about 5 weight percent, based on the total weight of the contents of the carbonylation reactor. Since the quantity of the acetone produced is relatively small, its value is not sufficient to justify the cost of its separating and purifying it to a sales grade acetone product. However, the acetone by-product in the process methyl acetate and methyl iodide recycle streams can lead to further undesirable by-products and/or reduction of the overall process efficiency. Among other things, acetone has been reported to inhibit the process catalyst. Acetone also forms "reducing substances" which cause quality problems in the acetic anhydride product.
  • U.S. Patent. No. 4,444,624 describes a system similar to the process of the '748 patent wherein a portion of the low boiler effluent is distilled with a countercurrent of acetic acid to give a fraction rich in methyl iodide and methyl acetate and a second fraction rich in methyl acetate and acetone, both of which contain very large quantities of acetic acid.
  • the acetone-containing fraction is further distilled to give a fraction containing primarily methyl acetate and most of the acetone.
  • the ratio of methyl acetate to acetone is very high, generally about 50: 1.
  • the acetone is removed from the larger amount of methyl acetate by azeotropic distillation with pentane and subsequent aqueous extraction to remove the acetone.
  • This process employs very large volumes of acetic acid, generally around 1 part of acetic acid for every 2 parts of low boiler fraction to be extractively distilled, and entails 4 operational steps (3 distillations and extraction.).
  • This process requires one less step than the process of the '748 patent only because it does not attempt to purify the acetone from the acetone- water mixture.
  • the processes of both the 748 and '624 patents require the use of pentane which introduces the risk of product contamination since pentane is not otherwise used in the acetic anhydride production system.
  • U.S. Patent. No. 4,717,454 discloses a process where acetone may be removed by converting it to condensation products which may be removed from the production system in the distillation as part of the ethylidene diacetate. This patent allows the acetone concentration to reach an equilibrium in the reaction system.
  • U.S. Patent No. 5,057,192 discloses a process for the removal of acetone from the acetic anhydride production system in which the low boiling stream having methyl acetate, methyl iodide, acetic acid and acetone is distilled.
  • the process includes (1) obtaining from the production system a low-boiling stream comprising methyl acetate, methyl iodide, acetic acid and acetone; (2) distilling the stream of step (1) to obtain: (a) an overhead stream comprising methyl acetate, methyl iodide and acetone; and (b) an underflow stream comprising methyl acetate, methyl iodide, acetone and essentially all of the acetic acid; (3) extracting the step(2)(a) stream with water to obtain: (a) a methyl iodide phase containing methyl acetate; and (b) an aqueous phase containing methyl acetate, methyl iodide and acetone; and (4) distilling the aqueous phase to obtain: (a) a vapor phase comprising methyl acetate, methyl iodide and minor amounts of acetone and water; and (b) an aqueous stream containing methyl acetate and acetone.
  • U.S Patent No. 5,244,545 discloses a process for the removal of acetone from the acetic anhydride production system.
  • the process includes the steps of: (1) obtaining from the production system a low-boiling stream comprising methyl acetate, methyl iodide, acetic acid and acetone; (2) distilling the stream of Step (1) to obtain: (a) an overhead stream comprising methyl acetate, methyl iodide and acetone; and (b) an underflow stream comprising methyl acetate, methyl iodide, acetone and essentially all of the acetic acid; (3) (a) feeding the Step (2)(a) stream to the middle section of a distillation column; and (b) feeding water to the upper section of the distillation column; or, instead of steps (3)(a) and (3)(b), (c) feeding water to the Step (2)(a) stream and feeding the resulting mixture to the middle section of a distillation column; and (4) removing from the distillation column: (a
  • U.S. Patent No. 5,262,014 discloses a process for removing acetone from a mixture comprising acetone, methyl acetate and methyl iodide, the process includes the steps: (a) W wO ⁇ 0 ⁇ 1u/4w61 i 0w9 PCT/US00/30989
  • the process of the present invention provides a more efficient means for the removal of acetone using a minimum of steps and processing equipment without the loss of any significant amounts of materials in the acetone disposal stream.
  • the present invention is a process for the removal of acetone from a mixture which includes a methyl halide promoter, preferably methyl iodide, wherein the mixture includes methyl acetate, methyl iodide and acetone.
  • the mixture is from a carbonylation process where acetic anhydride and acetic acid is produced by contacting carbon monoxide with a mixture comprising methyl iodide and methyl acetate and/or dimethyl ether in the presence of a catalyst system, such as rhodium, which includes a methyl halide promoter.
  • the process of the present invention includes the steps: (1) introducing a mixture which includes acetone, methyl acetate and methyl iodide into a first distillation zone; (2) withdrawing a side stream having acetone, methyl acetate and methyl iodide from the first distillation zone; (3) introducing the side stream into a second distillation zone; (4) introducing water into the second distillation zone at substantially the same feed point as the side stream feed or at one or more points above the side stream feed; and (5) removing an overhead product comprising methyl acetate and substantially all of the methyl iodide fed to the second distillation zone and at one or more points below the side stream feed point an underflow product comprising acetone, methyl acetate and water.
  • the process of the present invention allows a greater quantity of acetone to be removed from the smaller quantity of low boiling material from an acetic anhydride production system.
  • smaller equipment can be used to remove acetone with reduced capital and operating expenses.
  • FIG. 1 illustrates a schematic illustration of one embodiment of the process in which a mixture containing acetone, methyl acetate, acetic acid and methyl iodide is introduced to a first distillation column; a side stream is withdrawn having acetone, methyl acetate and methyl iodide from the middle zone of the first distillation column; the side stream is introduced into a second distillation column; water is introduced into the second distillation column at substantially the same feed point as the side stream feed or at one or more points above the side stream feed; and overhead product is removed from the second distillation column comprising methyl acetate and substantially all of the methyl iodide fed to the second distillation column and at one or more points below the side stream feed point an underflow product comprising acetone, methyl acetate and water is removed.
  • FIG. 2 is an illustration of another embodiment of the process of the present invention where a side stream comprising methyl acetate, water and essentially all of the acetone fed to the second distillation column is withdrawn and where a portion of a liquid bottom stream comprising essentially water is recycled to the water feed point for the second distillation column.
  • FIG. 3 is an illustration of another embodiment of the process of the present invention where a portion of the overhead stream from the first distillation column is contacted with water in an aqueous extraction column to produce a product stream having methyl acetate, methyl iodide, acetone and water.
  • FIG. 4 is an illustration of another embodiment of the process of the present invention where in addition to the side stream and liquid bottom stream being withdrawn from the second distillation column, a portion of the liquid bottom stream is used in an aqueous extraction column to produce a product stream having methyl acetate, methyl iodide, acetone and water and/or is recycled to the water feed point for the second distillation column.
  • a low-boiling mixture comprising methyl acetate, methyl iodide, acetic acid and acetone is fed by conduit 10 to a first distillation column 12.
  • the low boiling mixture may be obtained from the acetic anhydride production system described in Example 1 of U.S. Pat. No. 4,374,070, as well as other known acetic anhydride manufacturing processes.
  • the low boiling mixture is the portion of the reactor effluent remaining after removal of the catalyst components, a substantial amount of the low boiling components and essentially all of the acetic anhydride and higher boiling by-products.
  • the low boiling mixture consists of about 75 to 45 weight percent methyl acetate, 30 to 15 weight percent methyl iodide and 20 to 5 weight percent acetic acid with the concentration of the acetone varying from about 8 to 4 weight percent, depending on the length of time the acetone removal process has been operated.
  • the mixture also may contain a trace, e.g., about 0.1 to 0.5 weight percent, of acetic anhydride. While the mixture may contain significant amounts, e.g., 30 to 40 weight percent of acetic anhydride, the preferred process normally is carried out using a mixture from which substantially all of the acetic anhydride and other high boilers such as ethylidene diacetate have been removed elsewhere in the production system.
  • Table 1 The boiling points of the volatile materials in the process are given in Table 1 below:
  • Mel is methyl iodide
  • MeOAc is methyl acetate
  • Mel/Acetone, Mel/MeOAc and MeOAC/Acetone are constant boiling mixtures (binary azeotropes) consisting of, by weight, 95% methyl iodide and 5% acetone, 97.3% methyl iodide and 2.7 methyl acetate, and 50% methyl acetate and 50% acetone, respectively.
  • Distillation column 12 is operated at ambient pressure, a base temperature of about 60° to 70°C maintained by a heat source such as reboiler 14, and a top temperature of about 40° to 50°C. to fractionate the low boiling mixture into (1) an overhead stream comprising methyl acetate, methyl iodide and acetone; (2) a side stream comprising methyl acetate, methyl iodide and acetone and (3) a bottom stream, i.e., a base product stream, comprising methyl acetate, methyl iodide, acetone and essentially all of the acetic acid, acetic anhydride and higher boilers fed to the column.
  • a heat source such as reboiler 14
  • a top temperature of about 40° to 50°C.
  • the bottom stream is removed from distillation column 12 via conduit 16 and may be recycled to the carbonylation reactor along with additional methyl acetate, methyl iodide and catalyst components.
  • the primary function of column 12 is to remove all, or essentially all, of the acetic acid from the low boiling mixture. To accomplish this objective, a substantial portion of the methyl iodide and acetone fed to column 12 is removed with the acetic acid.
  • the vaporized overhead stream is removed from distillation column 12 by means of conduit 18 and passed through condenser 20 wherein substantially all of the stream is converted to a liquid.
  • a portion of the condensate from condenser 20 may be returned via lines 22 and 24 as reflux to distillation column 12.
  • the remainder of the condensate may be recycled to the carbonylation system via line 26.
  • a side stream comprising methyl acetate, methyl iodide and acetone is removed from distillation column 12 via line 28 and is passed through condenser 30 to convert substantially all of the constituents of the stream to a liquid phase.
  • the side stream 28 desirably has a ratio of acetone / methyl iodide of from 1 :20 and preferably from 1 : 10 and more preferably from 1 :8.5 which advantageously allows for greater acetone removal from a smaller quantity of low-boiling material.
  • the side stream, exiting the condenser 30, is fed via line 36 to a second distillation column or fractional distillation column 38. Desirably, the side stream 36 has a feed point at or near the middle of the second distillation column 38.
  • a portion of the condensate from the overhead of distillation column 12 not returned for reflux purposes, i.e., the material in line 26, can be combined with the side stream 36 before being introduced into the second distillation column 38, or the condensate in line 26 can be introduced at or substantially near the feed point of steam 36.
  • Water is introduced into the second distillation column 38 via line 39 at substantially the same feed point as the side stream feed 36 or at one or more points above the side stream feed 36.
  • the amount of water added to second distillation column 38 will depend upon such factors as the composition of the acetone / methyl acetate / methyl iodide mixture, the required compositions of the product streams and the number of separation stages in the distillation zone.
  • the ratio of water to mixture may suitably be from about 1 : 1 to about 10: 1.
  • the second distillation column 38 typically contains sufficient packing or other internals to provide a mass transfer adequate to remove essentially all the methyl iodide overhead, typically 8 to 20 ideal stages.
  • the second distillation column 38 operates at approximately ambient pressure, at a base temperature of about 98° to 105° C maintained by a reboiler 40 and a top temperature of about 45° to 55°C.
  • a vapor stream comprising methyl acetate, minor amounts of acetone and water, and essentially all of the methyl iodide, is removed from the top of distillation column 38 through line 42, condensed in condenser 44, and where at least a portion of the resulting liquid may be returned to distillation column 38 as reflux via line 46 or recycled to the carbonylation process by conduit 48.
  • the acetone removal system may be operated in a manner that produces a process effluent via line 50 which contains a methyl acetate: acetone weight ratio of not more than about 3:1, and preferably not more than about 1:1.
  • operation of the system provides for recovery of at least 95 weight percent, normally at least 99 weight percent, of the methyl iodide, the most valuable of the chemicals fed to the system.
  • the amount of iodine present in the process effluent removed from the system via line 50 desirably does not exceed 200 parts per million, and preferably is less than 100 ppm.
  • the lower section of fractional distillation column 38 is a liquid phase consisting substantially of water with the possibility of containing minute amounts of acetone and methyl acetate that collects at the bottom of the column.
  • the lower section of extractive distillation column 38 has less than about 5 total weight % of methyl acetate and acetone.
  • the liquid phase is drained from the base of column 38 through conduit 50 and a portion is fed to heat source 40 which is then recycled back to the base of the column to maintain a base temperature of about 90° to 95° C.
  • the remainder of the liquid phase is recycled, by means of line 51 , to the upper portion of extractive distillation column 38 and desirably to a point at or above the feed for side stream 36 and preferably is combined with the water feed line 39 prior to introducing the water into the second distillation column 38.
  • a second side stream is removed from the second distillation column 38 via line 52.
  • the second side stream 52 includes from about 75-95 weight % of the acetone fed to the second distillation column 38 via line 36 and more preferably from 80-95 weight % of acetone fed to the second distillation column 38 via line 36 with the remaining weight % comprising water and methyl acetate.
  • the second side stream 52 is condensed in condenser 54 and transported via line 56 to a suitable industrial waste treatment plant.
  • the first distillation column can be omitted and the low-boiling stream 10 can be fed directly to the fractionation distillation column 38.
  • the process of the present invention would include the steps of: (1) introducing a mixture which includes acetone, methyl acetate and methyl iodide into a distillation zone; (2) introducing water into the distillation zone at substantially the same feed point as the mixture feed stream or at one or more points above the mixture feed stream; and (3) removing from the distillation column (a) an overhead vapor stream comprising methyl acetate and essentially all of the methyl iodide fed to the distillation column; (b) a side stream having acetone, methyl acetate and water; and (c) an underflow or bottoms product consisting substantially of water.
  • FIG. 3 another embodiment of the present invention is illustrated and represents a process similar to that depicted in FIG. 1, except with the following modifications.
  • the portion of the condensate from condenser 20 not returned via lines 22 and 24 as reflux to distillation column 12 is fed by via line 26 to the upper portion of a counter-current, water extraction column 31.
  • Typical ratios for the amount of reflux to extractor feed, i.e., the conduit 24 reflux : conduit 26 extractor feed, are from about 2:1 to 10:1.
  • Water is fed to extraction column 31 via line 32 located near the bottom of extraction column 31.
  • the water extraction column 31 is typically equipped with four beds packed having 0.625 inch pall ring packing material.
  • the upwardly-flowing water extracts essentially all, e.g., at least 98 weight percent, of the acetone and a substantial portion, e.g., about 92 to 99 weight percent, of the methyl acetate.
  • a small amount, e.g., about 5 weight percent, of the methyl iodide fed to the water extractor column 31 overflows with the aqueous phase.
  • the remainder of the methyl acetate is removed from the base of water extraction column 31 via conduit 33 and may be recycled to the carbonylation reactor or used as the methyl iodide source in the tar removal process described in U.S. Pat. No. 4,388,217.
  • the methyl iodide stream obtained from water extractor 31 typically has a purity of at least 95 weight percent and preferably at least 98 weight percent.
  • the aqueous phase overflows extraction column 31 at or near the top and is transported through conduit 34, to the mid-section of fractional distillation column 38.
  • the aqueous phase overflow from the water extraction column 31 is fed to the fractional distillation column 38 at substantially the same feed point as the side stream feed 36, or may be combined with the side stream 36 prior to being introduced into the second distillation column 38, or may be introduced into the second distillation column 38 at one or more points above the side stream feed 36.
  • the bottoms of fractionating distillation column 38 is a liquid phase consisting substantially of water, and desirably comprises greater than about 95 weight % water and less than about 5 weight % total of methyl acetate and acetone.
  • the liquid bottoms of fractionating distillation column 38 comprises greater than about 98 weight % water and less than about 2 weight % total of methyl acetate and acetone.
  • the liquid phase is drained from the base of column 38 through conduit 50 and a portion is fed to heat source 40 which is then recycled back to the base of the column to maintain a base temperature of about 90° to 95° C.
  • the remainder of the liquid phase can be recycled, by means of line 51, to either (a) a feed point above the location of the side stream 36 feed point and/or above the aqueous stream 34 feed point; and /or (b) is used as the water source for the water extraction column 31 along with fresh water provided by a fresh water make-up line, not shown. Desirably, up to about 60 weight percent of the liquid phase transported by conduit 51 may be recycled to water extraction column 31 for use as the water source.
  • a second side stream is removed from the second distillation column 38 via line 52.
  • the second side stream 52 includes from about 75-95 weight % of the acetone fed to the second distillation column 38 via line 36 and more preferably from about 80-95 weight % of acetone fed to the second distillation column 38 via line 36 with the remaining weight % comprising water and methyl acetate.
  • the second side stream 52 is condensed in condenser 54 and transported via line 56 to a suitable industrial waste treatment plant.
  • the process of the present invention may be employed continuously or semi- continuously as necessary to lower the concentration of the acetone in the carbonylation reactor within a predetermined range.
  • acetic anhydride containing lower levels of reducing substances decreases the amount of bleaching agents required in cellulose acetate manufacturing processes, thereby lowering the manufacturing costs and further enhancing the value of the acetic anhydride.
  • the process provided by the present invention provides a means for producing, by the carbonylation processes described above, acetic anhydride which will more consistently pass the reducing substances test.
  • a feed mixture containing methyl acetate is continuously fed to a carbonylation reactor and a reaction product mixture containing acetic anhydride is continuously removed,
  • the feed to the reactor is such so as to maintain within the reaction mixture about 500 to 1000 ppm rhodium, about 1500 to 3700 ppm lithium, about 7 to 35 weight percent methyl iodide and about 5 to 40 weight percent acetic acid.
  • the effluent from the liquid phase carbonylation reactor is processed to remove unreacted carbon monoxide and other non-condensible gases and catalyst components. Any dimethyl ether fed to the carbonylation reactor which is not converted to methyl acetate is also removed as a component of the non-condensible gases. The remainder of the effluent is fed to a distillation column from which a crude acetic anhydride/acetic acid mixture is obtained.
  • the vaporized low-boiler stream removed at or near the top of the distillation column comprises methyl acetate, methyl iodide, acetic acid and acetone
  • the low-boiler stream is condensed and all or a portion, typically about 5 to 25 weight percent, of it is subjected to the acetone removal process of the present invention.
  • the low-boiler stream from carbonylation was fed through conduit 10 at a rate of 1000 parts to the lower midsection of distillation column 12.
  • Distillation column 12 was maintained by a heat source 14 at a base temperature of 60° to 65°C to give an acetic acid underflow or bottoms stream removed by line 16.
  • a vapor side stream was removed at a rate of 50 parts through conduit 28 and condensed in condenser 30. This material was then fed to the middle of distillation column 38 by means of conduit 36.
  • the vapor removed from the top of column 12 was condensed and a portion was returned to the column, via line 24, as reflux.
  • the balance of the condensate was transferred through conduit 26 to the upper part of water extraction column 31 at a rate of 200 parts.
  • Water was fed near the bottom of extractor 31 at a rate of 520 parts by conduit 32.
  • Methyl iodide having a purity near 99% was removed from the water extraction column by conduit 33.
  • the aqueous phase from the top of water extractor 31 was removed at a rate of 590 parts and was fed via line 34 to the middle of fractionation distillation column 38.
  • the side stream feed from distillation column 12 (line 36) feeds the fractionation distillation column 38 on the same tray.
  • the fractionation distillation column 38 was maintained at a base temperature of 95 to 100°C by heat source 40.
  • a vapor stream of methyl acetate, methyl iodide, and minor amounts of acetone and water was removed from distillation column 38 and condensed.
  • a portion of the condensate was returned through conduit 46 to the top of column 38 as reflux.
  • the balance of the condensate was returned via conduit 48 to the carbonylation system at a rate of 120 parts.
  • Water containing methyl acetate and acetone was removed from the bottom of the fractionation column 38 by line 50 at a rate of 520 parts.
  • the ratio of methyl acetate:acetone removed from the base of the column is in the range of 2: 1 to 1 :2.
  • compositions of streams transported by conduits 10, 26, 28, 34, 48, and 50 are given in Table 2 as weight percentages based on the total weight of the stream.

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  • Crystallography & Structural Chemistry (AREA)
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Abstract

La présente invention concerne un procédé permettant d"éliminer l"acétone d"un mélange d"acétate de méthyle, d"iodure de méthyle et d"acétone. Ce procédé consiste à éliminer un courant latéral à partir d"une zone de distillation qui est riche en acétone. Dans un mode de réalisation préféré de cette invention, le mélange d"acétate de méthyle, d"iodure de méthyle et d"acétone est mis en contact avec de l"eau, avant ou en même temps que la distillation fractionnée. Le procédé selon cette invention convient particulièrement à l"élimination de produit d"acétone dans un processus de carbonylation permettant la production d"anhydride acétique.
PCT/US2000/030989 1999-12-22 2000-11-13 Procede d"elimination amelioree d"acetone issue de processus de carbonylation WO2001046109A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
JP2001546623A JP2003518053A (ja) 1999-12-22 2000-11-13 カルボニル化プロセスからのアセトンの強化除去方法
BR0016571-9A BR0016571A (pt) 1999-12-22 2000-11-13 Processo para a remoção de acetona de uma mistura
EP00977156A EP1240128A1 (fr) 1999-12-22 2000-11-13 Procede d'elimination amelioree d'acetone issue de processus de carbonylation

Applications Claiming Priority (2)

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US46991199A 1999-12-22 1999-12-22
US09/469,911 1999-12-22

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WO2001046109A1 true WO2001046109A1 (fr) 2001-06-28

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EP2204357A1 (fr) 2009-01-06 2010-07-07 BP Chemicals Limited Procédé pour l'élimination de l'acétone d'un flux comprenant de l'acétone, de l'acétate de méthyle et de l'iodure de méthyle
CN104667556A (zh) * 2015-01-22 2015-06-03 宜兴市阳洋塑料助剂有限公司 一种用于生产增塑剂的精馏设备
EP3257833A4 (fr) * 2015-06-01 2018-03-28 Daicel Corporation Procédé de production d'acide acétique
CN113651695A (zh) * 2021-08-17 2021-11-16 天津天南同创科技发展有限公司 一种工业尾气制醋酸甲酯的分离精制方法

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CN101870644B (zh) * 2010-07-20 2013-01-23 张立省 羰基合成乙酸酐工艺中去除丙酮的装置
CN101891605B (zh) * 2010-07-20 2013-05-15 张立省 羰基合成乙酸酐工艺中去除丙酮的方法
CN103274922B (zh) * 2013-05-16 2015-01-14 南通大学 侧线精馏与共沸精馏集成分离丙酮-醋酸-水的方法

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EP2204357A1 (fr) 2009-01-06 2010-07-07 BP Chemicals Limited Procédé pour l'élimination de l'acétone d'un flux comprenant de l'acétone, de l'acétate de méthyle et de l'iodure de méthyle
WO2010079317A1 (fr) 2009-01-06 2010-07-15 Bp Chemicals Limited Procédé d'élimination de l'acétone d'un courant comprenant de l'acétone, de l'acétate de méthyle et de l'iodure de méthyle
US9233902B2 (en) 2009-01-06 2016-01-12 Bp Chemicals Limited Process for removing acetone from a stream comprising acetone, methyl acetate and methyl iodide
CN104667556A (zh) * 2015-01-22 2015-06-03 宜兴市阳洋塑料助剂有限公司 一种用于生产增塑剂的精馏设备
EP3257833A4 (fr) * 2015-06-01 2018-03-28 Daicel Corporation Procédé de production d'acide acétique
US20180118651A1 (en) * 2015-06-01 2018-05-03 Daicel Corporation Process for producing acetic acid
US10562836B2 (en) 2015-06-01 2020-02-18 Daicel Corporation Process for producing acetic acid
CN113651695A (zh) * 2021-08-17 2021-11-16 天津天南同创科技发展有限公司 一种工业尾气制醋酸甲酯的分离精制方法
CN113651695B (zh) * 2021-08-17 2024-02-06 天津天南同创科技发展有限公司 一种工业尾气制醋酸甲酯的分离精制方法

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