WO2000069802A1 - Method for producing vinyl acetate monomer from ethane or ethylene oxidation - Google Patents

Method for producing vinyl acetate monomer from ethane or ethylene oxidation Download PDF

Info

Publication number
WO2000069802A1
WO2000069802A1 PCT/EP2000/004234 EP0004234W WO0069802A1 WO 2000069802 A1 WO2000069802 A1 WO 2000069802A1 EP 0004234 W EP0004234 W EP 0004234W WO 0069802 A1 WO0069802 A1 WO 0069802A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst
ethylene
ethane
acetic acid
vinyl acetate
Prior art date
Application number
PCT/EP2000/004234
Other languages
French (fr)
Other versions
WO2000069802A9 (en
Inventor
Khalid Karim
Alaa E. M. Adris
Original Assignee
Saudi Basic Industries Corporation
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=23212532&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2000069802(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Saudi Basic Industries Corporation filed Critical Saudi Basic Industries Corporation
Priority to US10/031,808 priority Critical patent/US6605739B1/en
Priority to EP00936733A priority patent/EP1180092B1/en
Priority to JP2000618222A priority patent/JP2002544250A/en
Priority to DE60023132T priority patent/DE60023132T2/en
Priority to AT00936733T priority patent/ATE306467T1/en
Publication of WO2000069802A1 publication Critical patent/WO2000069802A1/en
Publication of WO2000069802A9 publication Critical patent/WO2000069802A9/en

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/04—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds
    • C07C67/05—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds with oxidation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/04—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds
    • C07C67/05—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds with oxidation
    • C07C67/055—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds with oxidation in the presence of platinum group metals or their compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

  • the invention relates to improved integrated methods of making vinyl acetate monomers from ethane or ethylene using metal oxide catalysts. Description of the Related Art
  • lower alkanes C.-C as feed stock to produce value added petrochemicals
  • Lower alkanes are low cost and environmentally acceptable because of their low chemical reactivity.
  • Vinyl acetate monomer (VAM) is a well-known industrial chemical.
  • VAM Vinyl acetate monomer
  • the production of VAM from ethylene, oxygen and acetic acid using conventional VAM catalysts is known in the art.
  • VAM is typically used as a raw material for vinyl resins such as polyvinyl acetate.
  • VAM was previously primarily manufactured from the vapor phase reaction of ethylene, acetic acid and oxygen with a zinc acetate catalyst.
  • VAM has been produced from the vapor- phase reaction of ethylene, acetic acid and oxygen, with a palladium catalyst.
  • VAM may be made from ethylene wherein the first step involves reacting the ethylene to form acetic acid, followed by a second step of reacting a mixture of the acetic acid and ethylene to form vinyl acetate .
  • PCT Patent Publication WO 98/05620 describes the production of acetic acid and/or vinyl acetate from ethylene (or ethane) using a first catalyst active for the oxidation of ethylene to acetic acid and/or active for the oxidation of ethane to acetic acid, ethylene and carbon monoxide, and a second catalyst active for the production of vinyl acetate.
  • the patent also describes an additional necessary step for conversion of carbon monoxide to carbon dioxide. This is because carbon monoxide is poisonous to the VAM catalyst .
  • U.S. Patent No. 4,188,490 relates to a catalytic oxidation process for the production of mixtures of acetic acid and vinyl acetate comprising the step of contacting a feed mixture containing ethylene, oxygen and water (as steam) with a catalyst composition to provide a mixture of acetic acid and vinyl acetate.
  • the catalyst system comprises a palladium metal on a zinc oxide support treated in the presence of a sulfur modifier.
  • the method requires the subsequent step of fractional distillation to separate the acetic acid from the vinyl acetate.
  • the acetic acid contained in the product mixture is converted in situ to an alkali metal salt such as sodium acetate.
  • the method also requires the step of treating the catalyst with the sulfur modifier by, for example, flowing moist air containing S0 2 over the catalyst at 200°C for about one hour.
  • vinyl acetate is produced catalytically from ethane feed stocks .
  • Another aspect of the invention relates to the production of vinyl acetate from ethylene.
  • the catalysts suitable for use in the methods of the invention are active and selective to the desired end product, vinyl acetate.
  • the catalytic process for the production of VAM from ethane involves two steps. In the first step, a catalyst (the "first catalyst") is used to provide the function of activation of ethane to ethylene and acetic acid. In the second step, ethylene and acetic acid are further oxidized to VAM in the presence of a conventional VAM catalyst (the "second catalyst").
  • Another preferred embodiment relates to a method of forming a stoichiometric mixture of ethylene and acetic acid using the first catalyst, which mixture can be directly fed into a vinyl acetate reactor containing the VAM catalyst without adjustments.
  • Yet another preferred embodiment relates to a catalytic method wherein ethylene or ethane is converted to vinyl acetate in a single stage reactor.
  • the preferred catalytic methods of the invention do not produce carbon monoxide. This is advantageous because carbon monoxide is not environmentally friendly and can have a significant impact on down stream separation costs, as well as on the poisoning of the VAM catalyst .
  • Figure 1 is a schematical representation of a ethane to VAM reaction scheme according to one embodiment of the invention.
  • Figure 2 is a schematical representation of a ethane to VAM reaction scheme according to another embodiment of the invention.
  • the invention relates to novel methods of producing vinyl acetate.
  • the first catalyst is used which provides the dual functions of (a) activation of ethane (or ethane/ethylene) to acetic acid and ethylene and (b) ethylene to acetic acid.
  • vinyl acetate is formed through further oxidation of ethylene with acetic acid in the presence of a second catalyst, the VAM catalyst.
  • the catalysts of the invention can also be used to provide an optimal feed to a vinyl acetate reactor.
  • the catalyst system suitable for the first step of the present invention can be formed from compositions including a catalyst (a) of the formula Mo a V b Nb c Pd d , wherein: a is 1 to 5 ; b is 0 to 0 . 5 ; c is 0 . 01 to 0 . 5 ; and d is 0 to 0.2.
  • the numerical values of a, b, c and d represent the relative gram-atom ratios of the elements Mo, V, Nb and Pd, respectively, in the catalyst.
  • the elements are preferably present in combination with oxygen in the form of various oxides.
  • Another catalyst system, catalyst (b) has a composition comprising the elements Mo, V, Pd, Nb, La, and X (where X is Al, Ga, Si, or Ge) in the form of oxides in the ratio Mo a V b La c Pd d Nb e X f wherein: a is 1 ; b is 0.01 to 0.9; c is > 0 to 0.2; d is > 0 to 0.2. e is > 0 to 0.2; and f is > 0 to 0.3.
  • the numerical values of a, b, c, d, e and f represent the relative gram-atom ratios of the elements Mo, V, Pd, La, Nb and X, respectively, in the catalyst.
  • the elements are preferably present in combination with oxygen in the form of various oxides .
  • catalyst (c) suitable for the invention is formed from a calcined composition of Mo a V b Nb c X d , wherein: X is at least one promoter element selected from the group consisting of: P, B, Hf, Te, and As; A is about 1 to 5;
  • d is about 0 to 0.1.
  • the numerical values of a, b, c and d represent the relative gram-atom ratios of the elements Mo, V, Nb and X, respectively, in the catalyst.
  • the elements are preferably present in combination with oxygen in the form of various oxides .
  • the first catalyst (catalysts (a) or (b) or (c) or mixtures thereof) and methods of making the first catalyst are set forth in copending U.S. Application Serial No. 08/932,075 (Attorney Docket No. 582815-2060), filed September 17, 1997, entitled "Catalysts for the Oxidation of Ethane to Acetic Acid, Processes of Making the Same and Processes of Using the Same"; U.S. Patent Application Serial No. 08/997,913 (Attorney Docket No.
  • One broad aspect of the invention relates to the production of vinyl acetate from ethane, ethylene or mixtures of ethane and ethylene.
  • the method utilizes a first catalyst ((a) or (b) or (c) or mixtures thereof) providing the functions of activation of ethane to acetic acid and ethylene and further oxidation of ethylene with acetic acid to vinyl acetate using a conventional VAM catalyst such as a Pd/Al catalyst.
  • a first catalyst ((a) or (b) or (c) or mixtures thereof) providing the functions of activation of ethane to acetic acid and ethylene and further oxidation of ethylene with acetic acid to vinyl acetate using a conventional VAM catalyst such as a Pd/Al catalyst.
  • a conventional VAM catalyst such as a Pd/Al catalyst
  • the methods of the invention produce vinyl acetate with zero (or nondetectable) or insignificant production of carbon monoxide.
  • one preferred aspect of the invention relates to a method which employs a catalyst designed in such way that it does not produce any CO, which saves the treatment step of converting CO to C0 2 .
  • One embodiment of the invention comprises reacting ethane with oxygen and water (e.g. steam) in the presence of a first catalyst ( (a) or (b) or (c) or mixtures thereof) to form a mixture containing ethylene and acetic acid which is then reacted to form vinyl acetate.
  • a first catalyst (a) or (b) or (c) or mixtures thereof) to form a mixture containing ethylene and acetic acid which is then reacted to form vinyl acetate.
  • the raw material used as the source for the ethane or ethylene/ethane can be a gas stream, which preferably contains at least five volume percent of ethane/ethylene.
  • the gas can also contain minor amounts of the C 3 -C 4 alkanes and alkenes, preferably less than five volume percent of each.
  • the gas stream can also contain major amounts, preferably more than five volume percent, of nitrogen, carbon dioxide, and water in the form of steam.
  • the reaction mixture useful in carrying out the process is generally from 5 to 50 moles % of ethane, 5 to 50 moles % of molecular oxygen either as pure oxygen or in the form of air, and optionally 2 to 50 moles % of water in the form of steam.
  • the amount of oxygen present may be a stoichiometric amount, or lower, of the hydrocarbons in the feed.
  • Other gases may be used as reaction diluents or heat moderators such as helium, nitrogen, and carbon dioxide .
  • the gaseous components of the reaction mixture are preferably uniformly admixed prior to being introduced into the reaction zone.
  • the components may be preheated, individually or after being mixed, prior to being introduced into the reaction zone.
  • the first reaction zone containing the first catalyst ( (a) or (b) or (c) or mixtures thereof) , generally has a pressure of from 15 to 500 psi, preferably from 150 to 350 psi; a temperature of from about 100°C to about 450°C, preferably from 200°C to 350°C, more preferably from 250°C to 300°C; a contact time between the reaction mixture and the catalyst of from about 2 seconds to about 100 seconds, preferably from 5 seconds to 30 seconds; and a space hourly velocity of from about 50 to about 50,000 h "1 , preferably from 100 to 10,000 h "1 and most preferably from 200 to 3,000 h "1 .
  • the process occurs in two stages.
  • a mixture comprising ethane or ethylene, oxygen or a compound capable of providing oxygen and water (e.g., steam) is reacted to form a mixture containing ethylene, acetic acid, oxygen and water (e.g., steam).
  • the product mixture of the first stage is then fed into the second stage and reacted to produce vinyl acetate.
  • the feed from the first stage may be adjusted prior to being introduced into the second stage.
  • the oxygen, ethylene and acetic acid concentration may be adjusted to optimize the catalytic reaction.
  • the first stage of the process produces a stoichiometric composition of acetic acid and ethylene as a feed for the second stage .
  • adjustments of the feed for the second reactor are not required as the mixture produced in the first stage can be directly fed into the second stage.
  • a dual-function catalyst can be used in the first stage to provide the feed stock for the second stage, which may contain a conventional Pd/Al VAM catalyst or any catalyst suitable for converting the feed stock of acetic acid and ethylene to VAM.
  • VAM can also be directly produced from only ethane, oxygen and water without additional components since the outlet of the first reactor may be optimized to contain a stoichiometric mixture of acetic acid, - 1 2 -
  • ethylene and oxygen which is the feed mixture for the second reactor.
  • the temperature and pressure of the feed from the first stage are also not adjusted prior to the second stage .
  • the output from either the first or second stage is recycled into the same or an earlier stage.
  • the output from stage 1 may be recycled into stage 1 or the output from stage 2 may be recycled into stage 1 and/or stage 2.
  • the reaction zone comprises multiple stages of bilayered catalyst consisting of layers of a first catalyst ( (a) or (b) or (c) or mixtures thereof) according to the invention and a second conventional vinyl acetate catalyst.
  • the first catalyst converts ethane to a mixture of acetic acid and ethylene, preferably to an optimal mixture
  • the second catalyst converts the ethylene/acetic acid to vinyl acetate in a single reaction zone .
  • one preferred embodiment relates to a process carried out in a single stage with all the reactants being supplied as a single feed with unreacted initial reactants being recycled.
  • multiple stage addition of oxygen to the reactor with an intermediate hydrocarbon feed can also be used. This may improve productivity to vinyl acetate and avoid potentially hazardous conditions.
  • Two possible integrated schemes using the first catalyst and the second VAM catalyst for direct production of VAM from ethane or ethane/ethylene mixtures without producing carbon monoxide are shown in Figures 1 and 2.
  • the liquid stream from gas/liquid separation unit 2 goes to distillation unit 3, where acetic acid is separated from water or the liquid stream from gas/liquid separation unit 2 can directly go to VAM reactor 5 containing a conventional VAM catalyst (CAT-B) .
  • VAM reactor 5 containing a conventional VAM catalyst (CAT-B) .
  • the treated gases consisting of ethane, ethylene and oxygen and the liquid stream consisting of acetic acid or acetic acid and water are fed to VAM reactor 5 to produce VAM, C0 2 and unreacted ethane, ethylene and acetic acid.
  • the effluent of VAM reactor 5 is then fed to gas liquid separation unit 6 where gases including ethane, ethylene and C0 2 are separated, partially purged to control the build up of non reacting species in purge unit 8 and recycled back to partial oxidation reactor 1.
  • the liquids are sent to distillation unit 7 for recovery of VAM. Acetic acid or unreacted acetic acid is recycled back to VAM reactor 5.
  • FIG. 2 is a schematical representation of reaction scheme B according to another embodiment of the invention.
  • the partial oxidation reactor 21 containing the first catalyst (CAT- A) converts fresh and recycled ethane or ethane/ethylene with oxygen into ethylene, acetic acid and carbon dioxide.
  • the effluent of reactor 21 is fed to VAM reactor 23 containing the VAM catalyst (CAT-B) via optional heat exchanger 22, which allows adjustment of the temperature of the feed to VAM reactor 23.
  • the two catalysts CAT-A and CAT-B can be in one reactor in the form of a physical mixture or in alternating layer form. Additional amounts of gases to VAM reactor 23, such as ethylene, acetic acid, and oxygen may be added depending upon the process conditions.
  • the effluent from VAM reactor 23 is fed to gas/liquid separation unit 24, where gases including C0 2 , C 2 H 4 , and C 2 H 6 are separated from liquid VAM, acetic acid and water.
  • the gas streams from gas/liquid separation unit 24 are recycled via carbon dioxide removal unit 25 to reactor 21.
  • the gas streams can also be recycled to reactor 21 without the absorption unit 25, as the catalyst CAT-A in the reactor 21 is not affected by the presence of carbon dioxide. Further, a specific amount of carbon dioxide also enhances the performance of the catalyst CAT-A. Gases are partially purged to control the build up of non reacting species in purge unit 27.
  • Liquid stream from separator unit 24 is fed to distillation unit 26 where acetic acid is separated from VAM and water and is optionally recycled to reactor 23 for make up or can be recovered.
  • VAM goes to a recovery unit and H 2 0 is recycled to reactor unit 21 for enhancement of acetic acid and selectivity.
  • Catalytic oxidation processes using a first catalyst were carried out in a tubular reactor under the following conditions . All experiments were run at the temperatures set forth below ranging from 260°C to 286°C, at a pressure of about 200 psig.
  • Reaction products were analyzed on-line by gas chromatography.
  • Oxygen, nitrogen and carbon monoxide were analyzed using a 3 mm by 3 mm column of 13X molecular sieve.
  • Carbon dioxide, ethane, ethylene and water were analyzed using a 1.8 m by 3mm column packed with material sold under the name HAYASEPTMQ.
  • Acetic acid was analyzed using a 0.5 m by 3 mm column packed with material sold under the name PORAPACKTM N.
  • stage I reactor Process conditions for stage I reactor: 286°C/200 psi
  • stage I reactor Process conditions for stage I reactor: 286°C/200 psi.
  • the catalytic methods used show high selectivity to vinyl acetate by oxidizing mixtures of ethane and ethylene .

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Catalysts (AREA)

Abstract

Methods for the catalytic production of vinyl acetate monomer from ethane, ethylene or an ethane/ethylene mixture using a first catalyst containing MoVNbPd, MoVLaPdNbX (where X is Al, Ga, Ge or Si) or MoVNbX (where X is P, B, Hf, Te, As or mixtures thereof) in the first step of oxidation and using a conventional VAM catalyst for the second step. The method produces high yields to acetic acid and vinyl acetate without the coproduction of carbon monoxide. Furthermore, the ethylene and acetic acid produced in the first step may be utilized in the second step for VAM production.

Description

TITLE OF THE INVENTION
METHOD FOR PRODUCING VINYL ACETATE MONOMER FROM ETHANE OR ETHYLENE OXIDATION
BACKGROUND OF THE INVENTION
Field of the Invention
The invention relates to improved integrated methods of making vinyl acetate monomers from ethane or ethylene using metal oxide catalysts. Description of the Related Art
Several publications are referenced in this application. These references describe the state of the art to which this invention pertains and are hereby incorporated by reference .
The utilization of lower alkanes (C.-C as feed stock to produce value added petrochemicals is an industrially desired process. Lower alkanes are low cost and environmentally acceptable because of their low chemical reactivity. There are only a few commercially available chemical catalytic processes, which utilize lower alkanes as a feed, such as butane to maleic anhydride .
Vinyl acetate monomer (VAM) is a well-known industrial chemical. The production of VAM from ethylene, oxygen and acetic acid using conventional VAM catalysts is known in the art. VAM is typically used as a raw material for vinyl resins such as polyvinyl acetate. VAM was previously primarily manufactured from the vapor phase reaction of ethylene, acetic acid and oxygen with a zinc acetate catalyst.
More recently, VAM has been produced from the vapor- phase reaction of ethylene, acetic acid and oxygen, with a palladium catalyst. For example, VAM may be made from ethylene wherein the first step involves reacting the ethylene to form acetic acid, followed by a second step of reacting a mixture of the acetic acid and ethylene to form vinyl acetate .
Numerous methods are known for the catalytic oxidation of ethylene to acetic acid. See, for example, U.S. Patent Nos . 3,792,087 and 3,970,697. Similarly, numerous methods are known for the catalytic production of vinyl acetate by reacting ethylene with acetic acid and oxygen in the gaseous phase. See, U.S. Patent Nos. 3,190,912; 3,637,819; 3,650,896; 4,370,492; 5,185,308; and 4,902,823.
PCT Patent Publication WO 98/05620 describes the production of acetic acid and/or vinyl acetate from ethylene (or ethane) using a first catalyst active for the oxidation of ethylene to acetic acid and/or active for the oxidation of ethane to acetic acid, ethylene and carbon monoxide, and a second catalyst active for the production of vinyl acetate. The patent also describes an additional necessary step for conversion of carbon monoxide to carbon dioxide. This is because carbon monoxide is poisonous to the VAM catalyst .
U.S. Patent No. 4,188,490 relates to a catalytic oxidation process for the production of mixtures of acetic acid and vinyl acetate comprising the step of contacting a feed mixture containing ethylene, oxygen and water (as steam) with a catalyst composition to provide a mixture of acetic acid and vinyl acetate. The catalyst system comprises a palladium metal on a zinc oxide support treated in the presence of a sulfur modifier. The method requires the subsequent step of fractional distillation to separate the acetic acid from the vinyl acetate. Alternatively, the acetic acid contained in the product mixture is converted in situ to an alkali metal salt such as sodium acetate. The method also requires the step of treating the catalyst with the sulfur modifier by, for example, flowing moist air containing S02 over the catalyst at 200°C for about one hour.
Several methods for producing vinyl acetate from ethylene result in the production of carbon monoxide. The production of carbon monoxide is disadvantageous because it is poisonous to the second stage catalyst. Moreover, carbon monoxide is also a less desirable by-product due to environmental law constraints. In order to avoid this problem, it is necessary to introduce another catalytic reactor for the total oxidation of CO to C02. This can add significant costs to the catalytic process .
Accordingly, it would be desirable to provide an improved method for the selective production of vinyl acetate monomer from ethane without the production of carbon monoxide. OBJECTS OF THE INVENTION
It is an object of the invention to overcome the above- identified deficiencies.
It is another object of the invention to provide an improved catalytic method for the production of vinyl acetate.
It is a further object of the invention to provide an improved catalytic method for the oxidation of ethylene to produce vinyl acetate.
It is a further object of the invention to provide an improved catalytic method for the oxidation of ethane to produce vinyl acetate .
It is a still further object of the invention to provide an improved catalytic method for the oxidation of ethane, ethylene or a mixture of ethane and ethylene to produce vinyl acetate without the production of carbon monoxide as a byproduct .
It is yet another object of the invention to provide an improved catalytic method for the single stage oxidation of ethane or ethylene or mixtures thereof to vinyl acetate.
The foregoing and other objects and advantages of the invention will be set forth in or be apparent from the following description.
SUMMARY OF THE INVENTION
According to the present invention, vinyl acetate is produced catalytically from ethane feed stocks . Another aspect of the invention relates to the production of vinyl acetate from ethylene. The catalysts suitable for use in the methods of the invention are active and selective to the desired end product, vinyl acetate. The catalytic process for the production of VAM from ethane involves two steps. In the first step, a catalyst (the "first catalyst") is used to provide the function of activation of ethane to ethylene and acetic acid. In the second step, ethylene and acetic acid are further oxidized to VAM in the presence of a conventional VAM catalyst (the "second catalyst"). Another preferred embodiment relates to a method of forming a stoichiometric mixture of ethylene and acetic acid using the first catalyst, which mixture can be directly fed into a vinyl acetate reactor containing the VAM catalyst without adjustments. Yet another preferred embodiment relates to a catalytic method wherein ethylene or ethane is converted to vinyl acetate in a single stage reactor.
Advantageously, the preferred catalytic methods of the invention do not produce carbon monoxide. This is advantageous because carbon monoxide is not environmentally friendly and can have a significant impact on down stream separation costs, as well as on the poisoning of the VAM catalyst .
Other objects as well as aspects, features and advantages of the present invention will become apparent from a study of the present specification, including the claims, figures and specific examples . DESCRIPTION OF THE FIGURES
Figure 1 is a schematical representation of a ethane to VAM reaction scheme according to one embodiment of the invention.
Figure 2 is a schematical representation of a ethane to VAM reaction scheme according to another embodiment of the invention.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
The invention relates to novel methods of producing vinyl acetate. In the first step, the first catalyst is used which provides the dual functions of (a) activation of ethane (or ethane/ethylene) to acetic acid and ethylene and (b) ethylene to acetic acid. In the second step, vinyl acetate is formed through further oxidation of ethylene with acetic acid in the presence of a second catalyst, the VAM catalyst. According to one preferred embodiment, the catalysts of the invention can also be used to provide an optimal feed to a vinyl acetate reactor. That is, catalytically oxidizing ethane (or ethylene/ethane) to form a mixture containing the optimal stoichiometric mixture of ethylene and acetic acid for use as a feed to a vinyl acetate reactor containing the conventional VAM catalyst, such as a Pd/Al catalyst.
The catalyst system suitable for the first step of the present invention (the first catalyst) can be formed from compositions including a catalyst (a) of the formula MoaVbNbcPdd, wherein: a is 1 to 5 ; b is 0 to 0 . 5 ; c is 0 . 01 to 0 . 5 ; and d is 0 to 0.2. The numerical values of a, b, c and d represent the relative gram-atom ratios of the elements Mo, V, Nb and Pd, respectively, in the catalyst. The elements are preferably present in combination with oxygen in the form of various oxides.
Another catalyst system, catalyst (b) , has a composition comprising the elements Mo, V, Pd, Nb, La, and X ( where X is Al, Ga, Si, or Ge) in the form of oxides in the ratio MoaVbLacPddNbeXf wherein: a is 1 ; b is 0.01 to 0.9; c is > 0 to 0.2; d is > 0 to 0.2. e is > 0 to 0.2; and f is > 0 to 0.3. The numerical values of a, b, c, d, e and f represent the relative gram-atom ratios of the elements Mo, V, Pd, La, Nb and X, respectively, in the catalyst. The elements are preferably present in combination with oxygen in the form of various oxides .
Another catalyst system, catalyst (c) , suitable for the invention is formed from a calcined composition of MoaVbNbcXd, wherein: X is at least one promoter element selected from the group consisting of: P, B, Hf, Te, and As; A is about 1 to 5;
b is 1; c is about 0.01 to 0.5; and
d is about 0 to 0.1.
The numerical values of a, b, c and d represent the relative gram-atom ratios of the elements Mo, V, Nb and X, respectively, in the catalyst. The elements are preferably present in combination with oxygen in the form of various oxides .
The first catalyst (catalysts (a) or (b) or (c) or mixtures thereof) and methods of making the first catalyst are set forth in copending U.S. Application Serial No. 08/932,075 (Attorney Docket No. 582815-2060), filed September 17, 1997, entitled "Catalysts for the Oxidation of Ethane to Acetic Acid, Processes of Making the Same and Processes of Using the Same"; U.S. Patent Application Serial No. 08/997,913 (Attorney Docket No. 582815-2080), filed December 24, 1997, entitled "Catalyst for Producing Acetic Acid from Ethane Oxidation, Processes of Making the Same and Methods of Using the Same" and U.S Serial No. 09/219,702, filed December 23, 1998, (Attorney Docket KR80577- 40) , entitled "Catalysts for the Oxidation of Ethane to Acetic Acid, Methods of Making and Using the Same", each of which is herein incorporated by reference . One broad aspect of the invention relates to the production of vinyl acetate from ethane, ethylene or mixtures of ethane and ethylene. The method utilizes a first catalyst ((a) or (b) or (c) or mixtures thereof) providing the functions of activation of ethane to acetic acid and ethylene and further oxidation of ethylene with acetic acid to vinyl acetate using a conventional VAM catalyst such as a Pd/Al catalyst. Overall, the recycled yield for vinyl acetate can be greater than 95%.
Advantageously, the methods of the invention produce vinyl acetate with zero (or nondetectable) or insignificant production of carbon monoxide. Preferably, less than 0.1 wt% carbon monoxide is produced as an end product using the invention, more preferably less than 0.01% and most preferred no detectable carbon monoxide is produced. Accordingly, one preferred aspect of the invention relates to a method which employs a catalyst designed in such way that it does not produce any CO, which saves the treatment step of converting CO to C02.
One embodiment of the invention comprises reacting ethane with oxygen and water (e.g. steam) in the presence of a first catalyst ( (a) or (b) or (c) or mixtures thereof) to form a mixture containing ethylene and acetic acid which is then reacted to form vinyl acetate.
The raw material used as the source for the ethane or ethylene/ethane can be a gas stream, which preferably contains at least five volume percent of ethane/ethylene. The gas can also contain minor amounts of the C3-C4 alkanes and alkenes, preferably less than five volume percent of each. The gas stream can also contain major amounts, preferably more than five volume percent, of nitrogen, carbon dioxide, and water in the form of steam.
The reaction mixture useful in carrying out the process is generally from 5 to 50 moles % of ethane, 5 to 50 moles % of molecular oxygen either as pure oxygen or in the form of air, and optionally 2 to 50 moles % of water in the form of steam. The amount of oxygen present may be a stoichiometric amount, or lower, of the hydrocarbons in the feed. Other gases may be used as reaction diluents or heat moderators such as helium, nitrogen, and carbon dioxide .
The gaseous components of the reaction mixture are preferably uniformly admixed prior to being introduced into the reaction zone. The components may be preheated, individually or after being mixed, prior to being introduced into the reaction zone.
The first reaction zone, containing the first catalyst ( (a) or (b) or (c) or mixtures thereof) , generally has a pressure of from 15 to 500 psi, preferably from 150 to 350 psi; a temperature of from about 100°C to about 450°C, preferably from 200°C to 350°C, more preferably from 250°C to 300°C; a contact time between the reaction mixture and the catalyst of from about 2 seconds to about 100 seconds, preferably from 5 seconds to 30 seconds; and a space hourly velocity of from about 50 to about 50,000 h"1, preferably from 100 to 10,000 h"1 and most preferably from 200 to 3,000 h"1.
According to one preferred embodiment, the process occurs in two stages. In the first stage, a mixture comprising ethane or ethylene, oxygen or a compound capable of providing oxygen and water (e.g., steam) is reacted to form a mixture containing ethylene, acetic acid, oxygen and water (e.g., steam). The product mixture of the first stage is then fed into the second stage and reacted to produce vinyl acetate.
The feed from the first stage may be adjusted prior to being introduced into the second stage. For example, the oxygen, ethylene and acetic acid concentration may be adjusted to optimize the catalytic reaction. Preferably, the first stage of the process produces a stoichiometric composition of acetic acid and ethylene as a feed for the second stage . According to one particularly preferred embodiment, adjustments of the feed for the second reactor are not required as the mixture produced in the first stage can be directly fed into the second stage. Thus, a dual-function catalyst can be used in the first stage to provide the feed stock for the second stage, which may contain a conventional Pd/Al VAM catalyst or any catalyst suitable for converting the feed stock of acetic acid and ethylene to VAM.
Therefore, using the present invention, VAM can also be directly produced from only ethane, oxygen and water without additional components since the outlet of the first reactor may be optimized to contain a stoichiometric mixture of acetic acid, - 1 2 -
ethylene and oxygen which is the feed mixture for the second reactor. Preferably, the temperature and pressure of the feed from the first stage are also not adjusted prior to the second stage .
According to one embodiment, the output from either the first or second stage is recycled into the same or an earlier stage. For example, the output from stage 1 may be recycled into stage 1 or the output from stage 2 may be recycled into stage 1 and/or stage 2.
According to another embodiment, the reaction zone comprises multiple stages of bilayered catalyst consisting of layers of a first catalyst ( (a) or (b) or (c) or mixtures thereof) according to the invention and a second conventional vinyl acetate catalyst. In this manner, the first catalyst converts ethane to a mixture of acetic acid and ethylene, preferably to an optimal mixture, and the second catalyst converts the ethylene/acetic acid to vinyl acetate in a single reaction zone .
Accordingly, one preferred embodiment relates to a process carried out in a single stage with all the reactants being supplied as a single feed with unreacted initial reactants being recycled. However, multiple stage addition of oxygen to the reactor with an intermediate hydrocarbon feed can also be used. This may improve productivity to vinyl acetate and avoid potentially hazardous conditions. Two possible integrated schemes using the first catalyst and the second VAM catalyst for direct production of VAM from ethane or ethane/ethylene mixtures without producing carbon monoxide are shown in Figures 1 and 2.
Figure 1 is schematical representation of one reaction scheme A according to one embodiment of the invention. The partial oxidation reactor 1 containing the first catalyst (CAT-A) converts fresh and recycled ethane or ethane/ethylene with oxygen into ethylene, acetic acid and carbon dioxide. An optimum amount of water from distillation reactor 3 is also introduced to partial oxidation reactor 1 in order to increase the acetic acid selectivity. The effluent from partial oxidation reactor 1 enters a gas/liquid separation unit 2. The gas stream from gas/liquid separation unit 2 is recycled to partial oxidation reactor 1 or goes to carbon dioxide absorption unit 4, where C02 is removed. The liquid stream from gas/liquid separation unit 2 goes to distillation unit 3, where acetic acid is separated from water or the liquid stream from gas/liquid separation unit 2 can directly go to VAM reactor 5 containing a conventional VAM catalyst (CAT-B) . The treated gases consisting of ethane, ethylene and oxygen and the liquid stream consisting of acetic acid or acetic acid and water are fed to VAM reactor 5 to produce VAM, C02 and unreacted ethane, ethylene and acetic acid. The effluent of VAM reactor 5 is then fed to gas liquid separation unit 6 where gases including ethane, ethylene and C02 are separated, partially purged to control the build up of non reacting species in purge unit 8 and recycled back to partial oxidation reactor 1. The liquids are sent to distillation unit 7 for recovery of VAM. Acetic acid or unreacted acetic acid is recycled back to VAM reactor 5.
Figure 2 is a schematical representation of reaction scheme B according to another embodiment of the invention. The partial oxidation reactor 21 containing the first catalyst (CAT- A) converts fresh and recycled ethane or ethane/ethylene with oxygen into ethylene, acetic acid and carbon dioxide. The effluent of reactor 21 is fed to VAM reactor 23 containing the VAM catalyst (CAT-B) via optional heat exchanger 22, which allows adjustment of the temperature of the feed to VAM reactor 23. Optionally, the two catalysts CAT-A and CAT-B can be in one reactor in the form of a physical mixture or in alternating layer form. Additional amounts of gases to VAM reactor 23, such as ethylene, acetic acid, and oxygen may be added depending upon the process conditions. The effluent from VAM reactor 23 is fed to gas/liquid separation unit 24, where gases including C02, C2H4, and C2H6 are separated from liquid VAM, acetic acid and water. The gas streams from gas/liquid separation unit 24 are recycled via carbon dioxide removal unit 25 to reactor 21. Optionally, the gas streams can also be recycled to reactor 21 without the absorption unit 25, as the catalyst CAT-A in the reactor 21 is not affected by the presence of carbon dioxide. Further, a specific amount of carbon dioxide also enhances the performance of the catalyst CAT-A. Gases are partially purged to control the build up of non reacting species in purge unit 27. Liquid stream from separator unit 24 is fed to distillation unit 26 where acetic acid is separated from VAM and water and is optionally recycled to reactor 23 for make up or can be recovered. VAM goes to a recovery unit and H20 is recycled to reactor unit 21 for enhancement of acetic acid and selectivity.
EXAMPLES
The following examples are illustrative of some of the products and methods of making and using the same falling within the scope of the present invention. They are, of course, not to be considered in any way limitative of the invention. Numerous changes and modifications can be made with respect to the invention.
Catalytic oxidation processes using a first catalyst ( (a) or (b) or (c) or mixtures thereof) were carried out in a tubular reactor under the following conditions . All experiments were run at the temperatures set forth below ranging from 260°C to 286°C, at a pressure of about 200 psig.
Reaction products were analyzed on-line by gas chromatography. Oxygen, nitrogen and carbon monoxide were analyzed using a 3 mm by 3 mm column of 13X molecular sieve. Carbon dioxide, ethane, ethylene and water were analyzed using a 1.8 m by 3mm column packed with material sold under the name HAYASEP™Q. Acetic acid was analyzed using a 0.5 m by 3 mm column packed with material sold under the name PORAPACK™ N.
In all cases, the conversion and selectivity calculations were based on the stoichiometry.
Data for the stage I reaction mentioned in the examples is experimental and the production of vinyl acetate (VAM) data in the stage II is calculated based on 92% yield to VAM from ethylene (C-hem. Syst-pm 91-10. Oct. 1992, herein incorporated by reference) .
Example 1: The Production of VAM from Ethylene:
The first catalyst (catalyst (a) ) : MoV0396Nb0128PdxOy (where x=
1.90e-04 and y is based on the co-ordination valence)
Process conditions for stage I reactor: 286°C/200 psi
Process conditions for stage II reactor as described in reference Chem. Syr,tern 91-10- Oct. 1992.
Results data:
Figure imgf000018_0001
The nitrogen, C02 and water are diluents in the stage II reaction.
Example 2 : The Production of VAM from Ethane
First catalyst (catalyst (a) ) : MoV0.39SNb0.128P<i--Oy (where x is 1.90e-04 and y is based on the co-ordination valence)
Process conditions for stage I reactor: 286°C/200 psi.
Process conditions for stage II reactor as described in f-hp.ττι .qye-t-p-m 91 -If), Oct. 1992.
Results Data:
Figure imgf000019_0001
The nitrogen, C02 and water act as diluents in stage II
Example 3 : The Production of VAM from Ethane
First catalyst (catalyst (a) ) : Mo25VX 0Nb032Pd003Oy (where y is based on the coordination valence) Process conditions for stage I reactor: 260°C/200 psi
Process conditions for stage II reactor as described in Chem. fiyst-f-m 91-10, Oct. 1992.
Results Data:
Figure imgf000020_0001
The nitrogen, C02 and water act as diluents in stage II.
Based on the above-described catalytic data, the following general characteristics can be concluded for the methods of the invention:
1. The catalytic methods used show high selectivity to vinyl acetate by oxidizing mixtures of ethane and ethylene .
2. The catalytic methods used also show high selectivity to vinyl acetate by oxidizing ethane.
3. The catalytic method systems used produce vinyl acetate without the production of by-products such - -
as carbon monoxide. This advantage reduces the step of CO conversion to C02 in the conventional VAM process . The above description of the invention is intended to be illustrative and not limiting. Various changes or modifications in the embodiments described may occur to those skilled in the art. These can be made without departing from the spirit or scope of the invention.

Claims

CLAIMS :
1. A process for the production of vinyl acetate monomer comprising the steps of: (1) contacting a gaseous feed mixture of ethane or ethylene or ethane/ethylene, steam and a molecular oxygen containing gas in the presence of a first catalyst active for oxidation of ethane, ethylene or ethane/ethylene to produce a selective stream of acetic acid, ethylene, carbon dioxide and water and (2) converting a second feed mixture comprising ethylene, acetic acid and oxygen to vinyl acetate monomer in the presence of a second catalyst active for the production of vinyl acetate, wherein said process does not include an intermediate separation step to remove the CO between the two reaction steps.
2. The process of claim 1, wherein said process produces no carbon monoxide.
3. The process of claim 2, wherein the first oxidation catalyst is selected from the following catalyst compositions : a) a catalyst composition comprising the elements Mo, V, Nb, and Pd,in the form of oxides, in the ratio MoaVbNbcPdd wherein: a is 1 to 5; b is 0 to 0.5; c is 0.01 to 0.5; and d is > 0 to 0.2; b) a catalyst composition comprising the elements Mo, V, Pd, Nb, La and X, in the form of oxides, wherein X is Al, Ga, Si or Ge, in the ratio MoaNbLacPddNbeXf wherein: a is 1; b is 0.01 to 0.9; c is > 0 to 0.2, d is > 0 to 0.2 e is > 0 to 0.2; and f is > 0 to 0.3; and c) a catalyst composition comprising the elements Mo,V,Nb and X (where X is P, B, Hf, Te, As or mixtures thereof) in the form of an oxide, in the following ratio MoaVbNbcXd wherein: a is 1 to 5 ; b is > 0 to 0.1; c is 0.01 to 0.5; d is > 0 to 0.1.
4. The process of claim 2 , wherein said first catalyst consists essentially of catalyst composition (a) , catalyst composition (b) , catalyst composition (c) or mixtures thereof .
5. The process of claim 2, wherein said first catalyst and second catalyst are in the form of a fixed or fluidized bed or a solid moving bed reactor.
6. The process of claim 2, wherein said feed mixture is fed into a second reaction zone.
7. The process of claim 6, wherein the second feed mixture for the second step comprises ethylene, acetic acid, C02 and oxygen.
8. The process of claim 2 , wherein said feed mixture comprises molecular oxygen ranging from 0.1 to 25% by volume of the feed mixture .
9. The process of claim 2 , wherein said feed mixture is diluted with N2 in an amount ranging from 5 to 90% by volume.
10. The process of claim 2, wherein said feed mixture is diluted with steam in an amount ranging from 0 to 40% by volume .
11. The process of claim 2, wherein said feed mixture comprises from 1% to 95% by volume of ethane, ethylene or mixtures thereof.
12. The process of claim 2, wherein first step oxidation is achieved at a temperature of from 150 to 450°C, under a pressure of from 15 to 600 psi, and with a contact time between reaction mixture and the catalyst of from 0.1 to 60 seconds .
13. The process of claim 2, wherein said contacting comprises reacting ethane or ethane/ethylene with steam and oxygen or a compound capable of providing oxygen in the presence of said first catalyst in a first reaction zone to form a first product mixture comprising ethylene, oxygen, steam and acetic - -
acid and the said first product mixture is fed into a second reaction zone wherein the ethylene and acetic acid react to form vinyl acetate in the presence of said second reaction catalyst.
14. The process of claim 13, wherein said first product mixture is fed directly into said second reaction zone without adding additional components .
15. The process of claim 13 , wherein said first product mixture is fed into said second reaction zone with addition/adjustment of ethylene, acetic acid, oxygen or combinations thereof .
16. The process of claim 13 , wherein said first product mixture is subjected to temperature and/or pressure adjustments prior to being fed into said second reaction zone.
17. A process of producing vinyl acetate monomer comprising the step of catalytically oxidizing ethane to form vinyl acetate in a single reaction zone containing a first catalyst having activity for oxidation of ethane to ethylene and acetic acid and a second catalyst having activity for oxidation of ethylene with acetic acid to vinyl acetate, wherein said first catalyst is at least one catalyst selected from the following catalyst compositions: a) a catalyst composition comprising the elements Mo, V, Nb, and Pd in the form of oxides, in the ratio MoaVbNbcPdd wherein: a is 1 to 5 ; b is 0 to 0 . 5 ; c is 0 . 01 to 0 . 5 ; and d is > 0 to 0 . 2 ; b) a catalyst composition comprising the elements Mo, V, Pd, Nb, La and X, in the form of oxides, wherein X is Ga, Si, Al or Ge, in the ratio oaVbL--cPd<_NbeXf wherein: a is 1; b is 0.01 to 0.9; c is > 0 to 0.2; d is > 0 to 0.2 ; e is > 0 to 0.2; and f is > 0 to 0.3; and c) a catalyst composition comprising the elements Mo,V,Nb and X (where X is P, B, Hf, Te, As or mixtures thereof) in the form of an oxide, in the following ratio MoaVbNbcXd wherein: a is 1 to 5; b is > 0 to 0.1; c is 0.01 to 0.5; and d is > 0 to 0.1.
18. The process of claim 17, wherein said single reaction zone comprises a mixture of said first catalyst and said second catalyst. - -
19. The process of claim 17, wherein said single reaction zone comprises layers of said first reaction catalyst and said second catalyst.
20. The process of claim 2, wherein said process produces ethylene, acetic acid, VAM or combinations thereof.
PCT/EP2000/004234 1999-05-14 2000-05-09 Method for producing vinyl acetate monomer from ethane or ethylene oxidation WO2000069802A1 (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
US10/031,808 US6605739B1 (en) 1999-05-14 2000-05-09 Method for producing vinyl acetate monomer from ethane or ethylene oxidation
EP00936733A EP1180092B1 (en) 1999-05-14 2000-05-09 Method for producing vinyl acetate monomer from ethane or ethylene oxidation
JP2000618222A JP2002544250A (en) 1999-05-14 2000-05-09 Method for producing vinyl acetate monomer from ethane or ethylene oxidation
DE60023132T DE60023132T2 (en) 1999-05-14 2000-05-09 METHOD FOR PRODUCING VINYL ACETATE MONOMER BY ETHANE OR ETHYLENE OXIDATION
AT00936733T ATE306467T1 (en) 1999-05-14 2000-05-09 METHOD FOR PRODUCING VINYL ACETATE MONOMER BY ETHANE OR ETHYLENE OXYDATION

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US09/312,683 US6143921A (en) 1999-05-14 1999-05-14 Method for producing vinyl acetate monomer from ethane or ethylene oxidation
US09/312,683 1999-05-14

Publications (2)

Publication Number Publication Date
WO2000069802A1 true WO2000069802A1 (en) 2000-11-23
WO2000069802A9 WO2000069802A9 (en) 2001-11-29

Family

ID=23212532

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2000/004234 WO2000069802A1 (en) 1999-05-14 2000-05-09 Method for producing vinyl acetate monomer from ethane or ethylene oxidation

Country Status (10)

Country Link
US (3) US6143921A (en)
EP (1) EP1180092B1 (en)
JP (1) JP2002544250A (en)
KR (1) KR100609203B1 (en)
CN (1) CN1188387C (en)
AT (1) ATE306467T1 (en)
DE (1) DE60023132T2 (en)
ES (1) ES2250137T3 (en)
SA (1) SA99200395B1 (en)
WO (1) WO2000069802A1 (en)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6790983B1 (en) 2000-05-19 2004-09-14 Celanese International Corporation Integrated process for the production of vinyl acetate
US7091377B2 (en) 2002-10-17 2006-08-15 Basf Aktiengesellschaft Multimetal oxide materials
USRE43859E1 (en) 1999-05-14 2012-12-11 Saudi Basic Industries Corporation Method for producing vinyl acetate monomer from ethane or ethylene oxidation
WO2018114752A1 (en) 2016-12-19 2018-06-28 Shell Internationale Research Maatschappij B.V. Ethane oxidative dehydrogenation with co-production of vinyl acetate
WO2018114747A1 (en) 2016-12-19 2018-06-28 Shell Internationale Research Maatschappij B.V. Ethane oxidative dehydrogenation with co-production of vinyl acetate
EP4116283A1 (en) 2021-07-06 2023-01-11 Linde GmbH Method and system for producing vinyl acetate

Families Citing this family (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7189377B1 (en) * 1996-08-07 2007-03-13 Bp Chemicals Limited Apparatus for performing integrated process for reproduction of vinyl acetate and/or acetic acid using a fluidized bed
US6258992B1 (en) * 1999-09-17 2001-07-10 Saudi Basic Industries Corporation Gas phase catalytic oxidation of hydrocarbons to carboxylic acids and dehydrogenated products
CN1174807C (en) * 2000-10-10 2004-11-10 巴斯福股份公司 Method for producing an annular shell catalyst and use thereof for producing acrolein
GB0026243D0 (en) * 2000-10-26 2000-12-13 Bp Chem Int Ltd Process
GB0026241D0 (en) 2000-10-26 2000-12-13 Bp Chem Int Ltd Process
KR100887001B1 (en) * 2001-03-30 2009-03-04 셀 인터나쵸나아레 레사아치 마아츠샤피 비이부이 Process for preparing a group ?-metal containing catalyst, use thereof for preparing an alkenyl carboxylate
US6642173B2 (en) * 2001-04-25 2003-11-04 Rohm And Haas Company Catalyst
TW574071B (en) * 2001-06-14 2004-02-01 Rohm & Haas Mixed metal oxide catalyst
GB0200021D0 (en) * 2002-01-02 2002-02-13 Bp Chem Int Ltd Process
GB0205016D0 (en) * 2002-03-04 2002-04-17 Bp Chem Int Ltd Process
GB0205014D0 (en) * 2002-03-04 2002-04-17 Bp Chem Int Ltd Process
JP4421201B2 (en) * 2002-03-27 2010-02-24 シエル・インターナシヨナル・リサーチ・マートスハツペイ・ベー・ヴエー Method for preparing a catalyst, catalyst, and use of the catalyst
US7294734B2 (en) * 2003-05-02 2007-11-13 Velocys, Inc. Process for converting a hydrocarbon to an oxygenate or a nitrile
US7220390B2 (en) 2003-05-16 2007-05-22 Velocys, Inc. Microchannel with internal fin support for catalyst or sorption medium
GB0312965D0 (en) 2003-06-05 2003-07-09 Bp Chem Int Ltd Process
TW201236755A (en) 2003-12-19 2012-09-16 Celanese Int Corp Halide free precursors for catalysts
US7465823B2 (en) * 2004-03-17 2008-12-16 Celanese International Corporation Utilization of acetic acid reaction heat in other process plants
KR100932575B1 (en) * 2004-12-20 2009-12-17 셀라니즈 인터내셔날 코포레이션 Modified support material for the catalyst
US8227369B2 (en) 2005-05-25 2012-07-24 Celanese International Corp. Layered composition and processes for preparing and using the composition
ATE442344T1 (en) * 2005-06-01 2009-09-15 Celanese Int Corp METHOD FOR SELECTIVE OXIDATION OF ETHANE TO ETHYLENE
DE102007025444A1 (en) * 2007-05-31 2008-12-11 Süd-Chemie AG VAM shell catalyst, process for its preparation and its use
DE102007025443A1 (en) 2007-05-31 2008-12-04 Süd-Chemie AG Pd / Au coated catalyst containing HfO 2, process for its preparation and its use
DE102007025362A1 (en) * 2007-05-31 2008-12-11 Süd-Chemie AG Doped Pd / Au coated catalyst, process for its preparation and its use
DE102007025223A1 (en) * 2007-05-31 2008-12-04 Süd-Chemie AG Zirconia-doped VAM shell catalyst, process for its preparation and its use
DE102007025315A1 (en) * 2007-05-31 2008-12-11 Süd-Chemie AG Catalyst for the selective hydrogenation of acetylenic hydrocarbons and process for its preparation
DE102007025442B4 (en) * 2007-05-31 2023-03-02 Clariant International Ltd. Use of a device for producing a coated catalyst and coated catalyst
DE202008017277U1 (en) 2008-11-30 2009-04-30 Süd-Chemie AG catalyst support
CA2828727A1 (en) 2011-03-02 2012-09-07 Mark Allen Nunley Methods for integrated natural gas purification and products produced therefrom
DE102012205444A1 (en) 2012-04-03 2013-10-10 Wacker Chemie Ag Process for the preparation of vinyl acetate
US11883798B2 (en) 2018-09-17 2024-01-30 Sabic Global Technologies B.V. Selective oxidation catalyst and a method for oxidizing C2 hydrocarbons in the presence of the selective oxidation catalyst
WO2020194228A1 (en) * 2019-03-26 2020-10-01 Sabic Global Technologies B.V. Method of reactivating catalyst

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19630832A1 (en) * 1996-07-31 1998-02-05 Hoechst Ag Process for the selective production of acetic acid
WO1998005620A1 (en) * 1996-08-07 1998-02-12 Bp Chemicals Limited Integrated process for the production of vinyl acetate and/or acetic acid
WO1999013980A1 (en) * 1997-09-17 1999-03-25 Saudi Basic Industries Corporation Catalysts for the oxidation of ethane to acetic acid, processes of making same and processes of using same

Family Cites Families (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3190912A (en) * 1962-05-02 1965-06-22 Nat Distillers Chem Corp Process for preparing esters
US3637819A (en) * 1967-12-30 1972-01-25 Knapsack Ag Process for the manufacture of unsaturated esters of carboxylic acids
US3650896A (en) * 1969-10-09 1972-03-21 Atomic Energy Commission Nuclear fuel particles
US3792087A (en) * 1971-11-10 1974-02-12 Nat Distillers Chem Corp Vapor phase oxidation of ethylene to acetic acid
US3970697A (en) * 1974-07-01 1976-07-20 National Distillers And Chemical Corporation Oxidation of ethylene to acetic acid
US4188490A (en) * 1977-05-27 1980-02-12 National Distillers And Chemical Corporation Catalytic oxidation of ethylene to mixtures of acetic acid and vinyl acetate
DE2811115A1 (en) * 1978-03-15 1979-09-27 Hoechst Ag CARRIER CATALYST FOR THE PRODUCTION OF VINYL ACETATE FROM ETHYLENE, ACETIC ACID AND OXYGEN IN THE GAS PHASE
DE3803900A1 (en) * 1988-02-09 1989-08-17 Hoechst Ag METHOD FOR PRODUCING VINYL ACETATE
US5185308A (en) * 1991-05-06 1993-02-09 Bp Chemicals Limited Catalysts and processes for the manufacture of vinyl acetate
US7189377B1 (en) * 1996-08-07 2007-03-13 Bp Chemicals Limited Apparatus for performing integrated process for reproduction of vinyl acetate and/or acetic acid using a fluidized bed
DE19717075A1 (en) 1997-04-23 1998-10-29 Hoechst Ag Process for the production of acetic acid in a reactor cascade
DE19745902A1 (en) * 1997-10-17 1999-04-22 Hoechst Ag Selective production of acetic acid with high space-time yield
US6030920A (en) 1997-12-24 2000-02-29 Saudi Basic Industries Corporation Catalysts for producing acetic acid from ethane oxidation, processes of making same and method of using same
US6028221A (en) 1998-06-29 2000-02-22 Saudi Basic Industries Corporation Catalyst systems for the one step gas phase production of acetic acid from ethylene and methods of making and using the same
US6060421A (en) 1998-12-23 2000-05-09 Saudi Basic Industries Corporation Catalysts for the oxidation of ethane to acetic acid, methods of making and using the same
US6143921A (en) 1999-05-14 2000-11-07 Saudi Basic Industries Corporation Method for producing vinyl acetate monomer from ethane or ethylene oxidation

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19630832A1 (en) * 1996-07-31 1998-02-05 Hoechst Ag Process for the selective production of acetic acid
WO1998005620A1 (en) * 1996-08-07 1998-02-12 Bp Chemicals Limited Integrated process for the production of vinyl acetate and/or acetic acid
WO1999013980A1 (en) * 1997-09-17 1999-03-25 Saudi Basic Industries Corporation Catalysts for the oxidation of ethane to acetic acid, processes of making same and processes of using same

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
USRE43859E1 (en) 1999-05-14 2012-12-11 Saudi Basic Industries Corporation Method for producing vinyl acetate monomer from ethane or ethylene oxidation
US6790983B1 (en) 2000-05-19 2004-09-14 Celanese International Corporation Integrated process for the production of vinyl acetate
EP1286945B2 (en) † 2000-05-19 2010-03-10 Celanese International Corporation Integrated process for the production of vinyl acetate
CZ303373B6 (en) * 2000-05-19 2012-08-22 Celanese International Corporation Integrated process for preparing vinyl acetate
US7091377B2 (en) 2002-10-17 2006-08-15 Basf Aktiengesellschaft Multimetal oxide materials
WO2018114752A1 (en) 2016-12-19 2018-06-28 Shell Internationale Research Maatschappij B.V. Ethane oxidative dehydrogenation with co-production of vinyl acetate
WO2018114747A1 (en) 2016-12-19 2018-06-28 Shell Internationale Research Maatschappij B.V. Ethane oxidative dehydrogenation with co-production of vinyl acetate
EP4116283A1 (en) 2021-07-06 2023-01-11 Linde GmbH Method and system for producing vinyl acetate
WO2023280947A1 (en) 2021-07-06 2023-01-12 Linde Gmbh Method and plant for the production of vinyl acetate

Also Published As

Publication number Publication date
JP2002544250A (en) 2002-12-24
SA99200395B1 (en) 2006-04-04
ES2250137T3 (en) 2006-04-16
EP1180092A1 (en) 2002-02-20
KR100609203B1 (en) 2006-08-02
US6605739B1 (en) 2003-08-12
WO2000069802A9 (en) 2001-11-29
US6143921A (en) 2000-11-07
KR20020015689A (en) 2002-02-28
DE60023132D1 (en) 2006-02-23
ATE306467T1 (en) 2005-10-15
CN1188387C (en) 2005-02-09
USRE43859E1 (en) 2012-12-11
EP1180092B1 (en) 2005-10-12
DE60023132T2 (en) 2006-06-29
CN1360565A (en) 2002-07-24

Similar Documents

Publication Publication Date Title
US6143921A (en) Method for producing vinyl acetate monomer from ethane or ethylene oxidation
US6143928A (en) Catalysts for low temperature selective oxidation of propylene, methods of making and using the same
JP2011116789A (en) Alkene separation method
US6258992B1 (en) Gas phase catalytic oxidation of hydrocarbons to carboxylic acids and dehydrogenated products
US6156928A (en) Method for gas phase production of acetic acid from ethane
EP1463709B1 (en) Integrated process for the manufacture of alkenyl carboxylates
US6028221A (en) Catalyst systems for the one step gas phase production of acetic acid from ethylene and methods of making and using the same
KR101006038B1 (en) Process for the production of an alkenyl carboxylate or an alkyl carboxylate

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): CN ID JP KR US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWE Wipo information: entry into national phase

Ref document number: 10031808

Country of ref document: US

ENP Entry into the national phase

Ref document number: 2000 618222

Country of ref document: JP

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: 1020017014540

Country of ref document: KR

AK Designated states

Kind code of ref document: C2

Designated state(s): CN ID JP KR US

AL Designated countries for regional patents

Kind code of ref document: C2

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE

COP Corrected version of pamphlet

Free format text: PAGES 1/2-2/2, DRAWINGS, REPLACED BY NEW PAGES 1/2-2/2; DUE TO LATE TRANSMITTAL BY THE RECEIVING OFFICE

WWE Wipo information: entry into national phase

Ref document number: 2000936733

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 008101868

Country of ref document: CN

WWP Wipo information: published in national office

Ref document number: 2000936733

Country of ref document: EP

WWP Wipo information: published in national office

Ref document number: 1020017014540

Country of ref document: KR

WWE Wipo information: entry into national phase

Ref document number: IN/PCT/2002/1289/KOL

Country of ref document: IN

WWG Wipo information: grant in national office

Ref document number: 2000936733

Country of ref document: EP

WWG Wipo information: grant in national office

Ref document number: 1020017014540

Country of ref document: KR