Celanese International Corporation

Hoechst Celanese Corporation

Celanese Gmbh

Other

Celanese International Corporaton

Jones, Kurt N.

Mark O Scates

Ronald David Shaver

Yaw-Hwa Liu

G Paull Torrence

Raymond J Zinobile

R Jay Warner

James H Zink

Heiko Weiner

Victor J Johnston

Josefina T Chapman

Yaw-Haw Liu

David E Lee

Dick Alan Nagaki

Craig J Peterson

Alexandra S Locke

Manuel Salado

Stephen Charles Webb

Valerie Santillan

Russell K Gibbs, Jr

Lincoln Sarager

Edward F Dougherty

Wayne David Picard

David A Trueba

Sarah Lane Abrego

Radmila Jevtic

George A Blay

Madan Singh

Jonathan A Makelki

Zhenhua Zhou

Adam Orosco

Tianshu Pan

James L Paul

Hung-Cheun Cheung

Oyeyemi F Oyerinde

Michael L Karnilaw

Elaine C Sibrel

Andrew Shuff

Duane Lyle Usrey

Pramod Agrawal

Richard F Vogel, Jr

Darrell Andrew Fisher

Trinity Horton

Radmila Wollrab

Jerry A Broussard

Emily Duff

Jeremy J Patt

Sean G Mueller

Melchior A Meilchen

Brian W Hokkanen

Charles C Hobbs, Jr

Barbara F M Kimmich

Leon B Levy

Robin Suzanne Tanke

G Paul Torrence

Steven E Parker

Melchior Albert Meilchen

Joshua Gregory Wagner

Jose J Arturo Talancon

Gregory Blanchard

Craig T Peterson

Jerome F Perez

Ronny G Wood

Jennifer B Lacy

Robert Glenn Golightly

Kenneth Paul Kidwell

Sean Mueller

Jose J Talancon

Robert Glenn Golighty

A process for producing an acetic acid product having low butyl acetate content via a carbonylation reaction. The carbonylation reaction is carried out at a temperature from 100 to 300&#xb0; C., a hydrogen partial pressure from 0.3 to 2 atm, and a metal catalyst concentration from 100 to 3000 wppm, based on the weight of the reaction medium. The butyl acetate concentration in the acetic acid product may be controlled by removing acetaldehyde from a stream derived from the reaction medium and/or by adjusting at least one of reaction temperature, hydrogen partial pressure, and metal catalyst concentration.

Processes for producing an acetic acid product having low butyl acetate content

Processes for purifying acetic acid by distilling a process stream in a column in which acetic anhydride is formed in the lower portion of the column. The product stream withdrawn from the column comprises acetic acid, water at a concentration of no more than 0.2 wt. %, and acetic anhydride at a concentration of no more than 600 wppm. The process further comprises hydrating the acetic anhydride in the product stream to form a purified acetic acid product comprising acetic anhydride at a concentration of no more than 50 wppm.

Processes for purifying acetic acid and hydrating anhydride

A process for producing acetic acid is disclosed in which the methyl iodide concentration is maintained in the vapor product stream formed in a flashing step. The methyl iodide concentration in the vapor product stream ranges from 24 to less than 36 wt. % methyl iodide, based on the weight of the vapor product stream. In addition, the acetaldehyde concentration is maintained within the range from 0.005 to 1 wt. % in the vapor product stream. The vapor product stream is distilled in a first column to obtain an acetic acid product stream comprising acetic acid and up to 300 wppm hydrogen iodide and/or from 0.1 to 6 wt. % methyl iodide and an overhead stream comprising methyl iodide, water and methyl acetate.

Process for flashing a reaction medium

A process for producing acetic acid is disclosed in which the recycle ratio of the mass flow of the light liquid phase recycled to the reactor to the mass flow of the aqueous recycle stream recycled to the reactor is less than or equal to 2.

Process to produce acetic acid with recycle of water

A process directed to acetic acid production comprising providing a feed stream comprising methyl iodide, water, acetic acid, methyl acetate, and at least one PRC to a distillation column comprising a distillation zone and a bottom sump zone and distilling the feed stream at a pressure and a temperature sufficient to produce an overhead stream comprising methyl iodide and at least one PRC, and a residuum stream flowing from the bottom sump zone comprising water and greater than or equal to about 0.11 weight percent HI is disclosed herein.

Process to control HI concentration in residuum stream

Process for producing acetic acid are disclosed in which a vapor sidedraw is withdrawn from the second column in the primary purification train. The vapor sidedraw comprises acetic acid and lithium-containing compounds at a concentration of no more than 100 wppb. A bottoms stream that is enriched in lithium-containing compounds, such as lithium acetate, or lithium acetate dihydrate, is also withdrawn from the second column. Advantageously, the vapor sidedraw, or a condensed portion thereof, is directly fed to a metal-exchanged ion exchange resin having acid cation exchange sites to produce purified acetic acid. This prevents displacement of the metals in the ion exchange resin.

Processes for producing acetic acid

Processes for purifying acetic acid by distilling a process in a column in which acetic anhydride is formed in the lower portion of the column. The product stream withdrawn from the column comprises acetic acid, water at a concentration of no more than 0.2 wt. %, and acetic anhydride at a concentration of no more than 600 wppm. The process further comprises hydrating the acetic anhydride in the product stream to form a purified acetic acid product comprising acetic anhydride at a concentration of no more than 50 wppm.

Processes for purifying acetic and hydrating anhydride

A process for producing acetic acid comprising the steps of carbonylating methanol in a reaction medium to form a crude acetic acid product; conveying the crude acetic acid product to a flash vessel at a flash flow rate; flashing the crude acetic acid product to form a first vapor stream comprising acetic acid and a liquid residue stream comprising metal catalyst and halide salt; separating the flashed vapor stream to form a second vapor stream comprising methyl iodide a sidedraw comprising purified acetic acid and water, and a liquid residue stream. The process further comprises the steps of condensing at least a portion of the second vapor stream to form at least one liquid phase and refluxing to the light ends column at least a portion of the at least one liquid phase at a reflux rate. The reflux rate is adjusted based on changes in the flash flow rate.

Processes for producing acetic acid with decanter control

In a process for improving a carbonylation process, iron is removed to maintain an effective Space Time Yield (STY) of the rhodium catalyst of at least 80% of the maximum STY. The process comprises carbonylating methanol in a reactor in a reaction medium comprising water, a rhodium catalyst, methyl iodide and a halide salt, separating a portion of the reaction medium in a flash vessel to form a less volatile stream and a vapor product stream comprising acetic acid, recycling a liquid stream to the reactor, wherein the liquid stream comprises a portion of the less volatile stream and wherein the liquid stream comprises iron, and removing a portion of the iron from the liquid stream to maintain an effective STY of the rhodium catalyst of at least 80% of the maximum STY.

Processes for improving acetic acid yield by removing iron

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Houston, TX, United States of America

Mark O Scates